CN114392639B - Catalytic cracking flue gas waste heat utilization coupling desulfurization wet smoke and rain elimination process - Google Patents
Catalytic cracking flue gas waste heat utilization coupling desulfurization wet smoke and rain elimination process Download PDFInfo
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- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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Abstract
The utility model relates to a catalytic cracking flue gas waste heat utilization coupling desulfurization wet smoke and rain elimination process, which can not only effectively utilize the flue gas waste heat, but also reduce the energy consumption in the catalytic cracking wet smoke and rain elimination process. The main embodiments are as follows: the condensation of the flue gas does not need an additional cold source, so that the system consumption is reduced; the absorption heat pump is adopted, so that low-temperature heat in the flue gas and the desulfurization circulating liquid is fully utilized, and the energy consumption of the system is reduced; the low-temperature heat in the desulfurization circulating liquid is converted into medium-temperature heat in the heat medium water by utilizing the absorption heat pump, so that the quality of the heat is improved, and the availability of the heat is further enhanced; the flue gas condensation reduces the consumption of the system supplementary water greatly.
Description
Technical Field
The utility model relates to the field of catalytic cracking flue gas purification, in particular to a catalytic cracking flue gas waste heat utilization coupling desulfurization wet smoke and rain elimination process.
Background
In recent years, along with serious environmental problems, the national emphasis on environmental problems is also growing, and the emission standard of an atmospheric pollution area is continuously improved, so that the environmental protection technology is continuously improved and advanced.
The flue gas discharged by the petroleum refining industry occupies a large proportion in the emission of atmospheric pollutants, wherein the flue gas discharged by the catalytic cracking device regenerator is the largest air pollution source of a refinery, and the flue gas comprises particulate matters, sulfur oxides, nitrogen oxides, carbon monoxide and the like. The catalytic cracking regeneration flue gas is generated by the following steps: carbon deposit is generated on the surface of the catalyst in the catalytic cracking and catalytic cracking reaction process, and the carbon deposit on the catalyst needs to be regenerated and burned out by entering a regenerator, so that the activity of the catalyst is recovered. The carbon deposit is burnt out by using air through a regenerator, the regenerated flue gas is discharged after the entrained catalyst is separated by a cyclone separator and the energy is recovered by a smoke machine and a waste heat boiler, and the catalytic cracking regenerated flue gas is generated in the process. The catalytic cracking regenerated flue gas has the characteristics of wide fluctuation range of sulfur content, large particle size range of particles, more content of particles below submicron level and the like.
In the prior art, aiming at catalytic cracking regeneration flue gas purification treatment, a wet removal process is generally adopted, and the regeneration flue gas is subjected to washing by a large amount of circulating absorption liquid to remove particulate matters and sulfides in the regeneration flue gas and then is discharged to the atmosphere. Because the wet method removing process is adopted, the exhaust smoke is saturated smoke and carries certain water vapor, and the wet smoke is contacted with the ambient air for cooling in the discharging process, obvious white smoke and even rain fall are formed, and the surrounding environment is influenced.
Meanwhile, in the catalytic cracking regeneration flue gas purification process, the flue gas waste heat is discharged by the waste heat recycling absorption liquid to absorb the waste heat of the flue gas, so that the wet flue gas and the waste heat of the circulating slurry are not utilized or are underutilized generally at present, and the flue gas waste heat is condensed and then heated in a mode of condensation before the flue gas waste heat is used, and the flue gas is heated by steam after the flue gas is condensed, so that the wet flue gas and the waste heat of the circulating slurry can be eliminated, but the energy consumption is high, the operation cost is high, and the application of the technology is limited.
Disclosure of Invention
The utility model aims to solve the technical problem of providing a technology for improving the utilization efficiency of catalytic cracking flue gas waste heat and coupling desulfurization wet flue gas and rain elimination, which can not only effectively utilize the flue gas waste heat, but also reduce the energy consumption in the process of eliminating the catalytic cracking wet flue gas and rain.
The technical scheme adopted for solving the technical problems is as follows:
a catalytic cracking flue gas waste heat utilization coupling desulfurization wet smoke and rain elimination process comprises the following steps:
the temperature of the catalytic cracking regenerated flue gas sent from the boundary region is 130-300 ℃, the pressure is 0.002-0.01 Mpag, the flue gas is subjected to primary washing absorption of a main absorption tower and secondary washing absorption of a comprehensive tower to remove sulfides and particulate matters in the flue gas, then the flue gas is sent to a demister to remove free water in the flue gas, the flue gas temperature is reduced to 50-80 ℃, and the flue gas is sent to a condensing section of the comprehensive tower;
the condensing section of the comprehensive tower is provided with a circulating pump and a circulating liquid cooler, circulating liquid in the condensing section of the comprehensive tower is pressurized to 0.3-1.0 Mpag through the circulating pump, is sent to the circulating cooler to be cooled to 35-55 ℃, is then sent to the condensing section of the comprehensive tower to be in direct spray contact with flue gas, the flue gas is cooled to 37-62 ℃, condensed water is produced by removing condensation of the flue gas through a secondary demister, the flue gas is mixed with hot air from an air heater, the temperature of the mixed flue gas is 50-85 ℃, the atmosphere is discharged, the treatment and discharge of wet smoke and rain are realized, the sprayed circulating liquid is sent to the circulating pump to be continuously utilized after being collected, and meanwhile, water from a boundary region is supplemented to the condensing section of the comprehensive tower for maintaining the water balance of the system;
the cold energy required by the circulating liquid cooler is provided by an absorption heat pump, the temperature of cooling water generated by the absorption heat pump is 10-30 ℃, the temperature is exchanged to 20-40 ℃ by the circulating liquid cooler, and the cooling water is pressurized to 0.1-1.0 Mpag by a cooling water pressurizing pump and then returned to the absorption heat pump for circulation cooling;
the air from the environment at normal temperature and normal pressure is pressurized by a fan, is heated to 60-90 ℃ by an air preheater, is sent to the air heater to be heated to 80-150 ℃, and is then sent to a smoke discharge port to be mixed with condensed smoke;
the heat required by the air preheater is provided by an absorption heat pump, the temperature of heat medium water generated by the absorption heat pump is 70-95 ℃, and the heat is exchanged to 55-75 ℃ by the air preheater and then returned to the absorption heat pump for cyclic heating.
Preferably, the low-pressure steam from the boundary region has a temperature of 130-200 ℃ and a pressure of 0.3-1.0 Mpag, and is divided into two parts, one part is sent to an air heater to be used as a heating source, and the other part is sent to the absorption heat pump to be used as driving heat, and the generated condensate is sent out of the boundary region; the absorption heat pump uses low-pressure steam as a driving source, low-temperature heat energy in circulating absorption liquid of a condensing section is transferred into heat medium water, the temperature of the heat medium water is 70-95 ℃, the heat medium water is pressurized to 0.1-1.0 Mpa by a heat medium water pressurizing pump and then divided into two parts, one part is sent to an air heater for heating air, the other part is sent out for use, and the mass flow ratio of the two parts of heat medium water is 1:9-1:2. The absorption heat pump uses a small amount of high-temperature steam as a driving heat source, and transfers low-temperature heat energy in the circulating absorption liquid into heat medium water, so that a large amount of medium-temperature useful heat energy is generated, namely, the absorption heat pump is driven by a small amount of high-temperature heat energy, and the heat energy of a large amount of low-temperature heat source is improved to the medium temperature, so that the utilization efficiency of the heat energy is improved, and the heat energy utilization rate is improved by 40% -70%.
Preferably, the ratio of the heat added by the heat medium water generated by the absorption heat pump to the heat of the circulating absorption liquid removed by the circulating cooler is 1.5:1-2.5:1.
Preferably, the utility model can also use hot water with the temperature of more than 90 ℃ as the driving heat source of the absorption heat pump.
Compared with the prior art, the utility model has the following advantages:
1. the condensation of the flue gas does not need an additional cold source, so that the system consumption is reduced;
2. the absorption heat pump is adopted, so that low-temperature heat in the flue gas and the desulfurization circulating liquid is fully utilized, and the energy consumption of the system is reduced;
3. the low-temperature heat in the desulfurization circulating liquid is converted into medium-temperature heat in the heat medium water by utilizing the absorption heat pump, so that the quality of the heat is improved, and the availability of the heat is further enhanced;
4. the flue gas condensation reduces the consumption of the system supplementary water greatly.
Drawings
FIG. 1 is a process flow diagram of example 1 of the present utility model;
FIG. 2 is a process flow diagram of example 2 of the present utility model.
Detailed Description
The utility model is described in further detail below with reference to the embodiments of the drawings.
Example 1:
as shown in fig. 1, the catalytic cracking flue gas waste heat utilization coupling desulfurization wet flue gas and rain elimination process of the embodiment comprises the following steps:
the temperature of the catalytic cracking regenerated flue gas sent from the boundary region is 180 ℃, the pressure is 0.005Mpag, the flue gas is washed and absorbed by a first section of a main absorption tower 2 and a second section 11 of a comprehensive tower, sulfide and particulate matters in the flue gas are removed, the flue gas is sent to a first-stage demister 12 to remove free water in the flue gas, the flue gas temperature is reduced to 55 ℃, and the flue gas is sent to a condensation section 13 of the comprehensive tower;
the comprehensive tower condensation section 13 is provided with a circulating pump 5 and a circulating liquid cooler 6, circulating liquid in the comprehensive tower condensation section is pressurized to 0.6Mpag through the circulating pump 5, is sent to the circulating cooler 6 to be cooled to 48 ℃, is then sent to the comprehensive tower condensation section 13 to be in direct spray contact with flue gas, the flue gas is cooled to 50 ℃, is subjected to condensation removal through a secondary demister 14 to generate condensation water, is mixed with hot air from an air heater 10, the temperature of the mixed flue gas is 75 ℃ below zero, the atmosphere is discharged, the treatment and discharge of wet smoke and rain are realized, the sprayed circulating liquid is continuously utilized by the circulating pump 5 after being collected, and meanwhile, the water from a boundary region is fed to the comprehensive tower condensation section 13 for maintaining the water balance of the system;
the cooling capacity required by the circulating liquid cooler 6 is provided by the absorption heat pump 7, the temperature of cooling water generated by the absorption heat pump 7 is 20 ℃, the cooling water exchanges heat to 30 ℃ through the circulating liquid cooler 6, and the cooling water returns to the absorption heat pump 7 for circulation cooling after being pressurized to 0.6Mpa through the cooling water pressurizing pump 11;
the air from the environment at normal temperature and normal pressure is pressurized by a fan 8, is heated to 70 ℃ by an air preheater 9, is sent to an air heater 10 to be heated to 120 ℃, and is sent to a flue gas discharge port to be mixed with condensed flue gas.
In this embodiment, the heat required by the air preheater 9 is provided by the absorption heat pump 7, the temperature of the heat medium water generated by the absorption heat pump 7 is 85 ℃, and the heat is exchanged to 60 ℃ by the air preheater 9 and then returned to the absorption heat pump for cyclic heating.
In the embodiment, the low-pressure steam from the boundary region has the temperature of 150 ℃ and the pressure of 0.6Mpag, and is divided into two parts, wherein one part is sent to the air heater 10 to serve as a heating source, and the other part is sent to the absorption heat pump 7 to serve as driving heat, so that the generated condensate is sent out of the boundary region; the absorption heat pump 7 uses low-pressure steam as a driving source, low-temperature heat energy in circulating absorption liquid in a condensing section is transferred into heat medium water, the temperature of the heat medium water is 85 ℃, the heat medium water is pressurized to 0.6Mpa by the heat medium water pressurizing pump 12 and then divided into two parts, one part is sent to the air heater 10 for heating air, the other part is sent out for use, and the mass flow ratio of the two parts of heat medium water is 1:2.
The ratio of the heat added by the heat medium water generated by the absorption heat pump 7 to the heat of the circulating absorption liquid removed by the circulating cooler 6 is 1.5:1.
The absorption heat pump 7 uses a small amount of high-temperature steam as a driving heat source to transfer low-temperature heat energy in the circulating absorption liquid to heat medium water, thereby generating a large amount of medium-temperature useful heat energy. The heat energy of a large amount of low-temperature heat sources is improved to medium temperature by using a small amount of high-temperature heat energy for driving, so that the utilization efficiency of the heat energy is improved, the consumption of low-pressure steam is reduced by 50%, and meanwhile, the circulating cooler 6 for condensing the flue gas adopts cooling water generated by the absorption heat pump 7, so that the consumption of an additional cold source is avoided, and the consumption is further reduced.
Example 2:
as shown in fig. 2, the catalytic cracking flue gas waste heat utilization coupling desulfurization wet flue gas and rain elimination process of the embodiment comprises the following steps:
the temperature of the catalytic cracking regenerated flue gas sent from the boundary region is 260 ℃, the pressure is 0.004Mpag, the flue gas is sent to a first-stage demister 12 to remove free water in the flue gas after being subjected to primary washing and absorption of a main absorption tower 2 to remove sulfides and particulate matters, the temperature of the flue gas is reduced to 62 ℃, and the flue gas is sent to a condensing section 13 of a comprehensive tower;
the comprehensive tower condensation section 13 is provided with a circulating pump 5 and a circulating liquid cooler 6, circulating liquid in the comprehensive tower condensation section is pressurized to 0.5Mpag through the circulating pump 5, is sent to the circulating cooler 6 to be cooled to 55 ℃, is then sent to the comprehensive tower condensation section 13 to be in direct spray contact with flue gas, the flue gas is cooled to 57 ℃, is subjected to condensation removal through a secondary demister 14 to generate condensation water, is mixed with hot air from an air heater 10, the temperature of the mixed flue gas is 80 ℃ to discharge the atmosphere, so that the treatment and discharge of wet smoke and rain are realized, the sprayed circulating liquid is continuously utilized by the circulating pump 5 after being collected, and meanwhile, the water from a boundary region is fed to the comprehensive tower condensation section 13 for maintaining the water balance of the system;
the cooling capacity required by the circulating liquid cooler 6 is provided by the absorption heat pump 7, the temperature of cooling water generated by the absorption heat pump 7 is 30 ℃, the cooling water exchanges heat to 40 ℃ through the circulating liquid cooler 6, and the cooling water returns to the absorption heat pump 7 for circulation cooling after being pressurized to 1.0Mpa through the cooling water pressurizing pump 11;
the air from the environment at normal temperature and normal pressure is pressurized by a fan 8, is heated to 85 ℃ by an air preheater 9, is sent to an air heater 10 to be heated to 120 ℃, and is sent to a flue gas discharge port to be mixed with condensed flue gas.
In this embodiment, the heat required by the air preheater 9 is provided by the absorption heat pump 7, and the temperature of the heat medium water generated by the absorption heat pump 7 is 95 ℃, and the heat is exchanged to 75 ℃ by the air preheater 9 and then returned to the absorption heat pump for cyclic heating.
In the embodiment, the temperature of hot water from the boundary region is 130 ℃, the pressure is 1.0Mpag, the hot water is divided into two parts, one part is sent to the air heater 10 to serve as a heating source, the other part is sent to the absorption heat pump 7 to serve as driving heat, and the driving heat returned from the absorption heat pump 7 is sent out of the boundary region at 80 ℃; the absorption heat pump 7 uses hot water as a driving source, low-temperature heat energy in circulating absorption liquid in a condensing section is transferred into heat medium water, the temperature of the heat medium water is 95 ℃, the heat medium water is pressurized to 1.0Mpa by the heat medium water pressurizing pump 12 and then divided into two parts, one part is sent to the air heater 10 for heating air, the other part is sent out of a boundary area for use, and the mass flow ratio of the two parts of heat medium water is 1:5.
The ratio of the heat added by the heat medium water generated by the absorption heat pump 7 to the heat of the circulating absorption liquid removed by the circulating cooler 6 is 2:1.
The absorption heat pump 7 uses a small amount of high-temperature steam as a driving heat source to transfer low-temperature heat energy in the circulating absorption liquid to heat medium water, thereby generating a large amount of medium-temperature useful heat energy. The heat energy of a large amount of low-temperature heat sources is improved to medium temperature by using a small amount of high-temperature heat energy for driving, so that the utilization efficiency of the heat energy is improved, the low-pressure steam consumption is reduced by 67%, and meanwhile, the circulating cooler 6 for condensing the flue gas adopts cooling water generated by the absorption heat pump 7, so that the consumption of an additional cold source is avoided, and the consumption is further reduced.
Claims (1)
1. The catalytic cracking flue gas waste heat utilization coupling desulfurization wet smoke and rain elimination process is characterized by comprising the following steps of:
the temperature of the catalytic cracking regenerated flue gas sent from the boundary region is 130-300 ℃, the pressure is 0.002-0.01 Mpag, sulfide and particulate matters in the flue gas are removed through primary washing and absorption of a main absorption tower and secondary washing and absorption of a comprehensive tower, free water in the flue gas is removed through a primary demister, the temperature of the flue gas is reduced to 50-80 ℃, and the flue gas is sent to a condensing section of the comprehensive tower;
the condensing section of the comprehensive tower is provided with a circulating pump and a circulating liquid cooler, circulating liquid in the condensing section of the comprehensive tower is pressurized to 0.1-1.0 Mpag through the circulating pump, is sent to the circulating liquid cooler to be cooled to 35-55 ℃, is then sent to the condensing section of the comprehensive tower to be in direct spray contact with flue gas, the flue gas is cooled to 37-62 ℃, condensed water is produced by removing condensation of the flue gas through a secondary demister, the flue gas is mixed with hot air from an air heater, the temperature of the mixed flue gas is 50-85 ℃, the atmosphere is discharged, the treatment and discharge of wet smoke and rain are realized, the sprayed circulating liquid is sent to the circulating pump to be continuously utilized after being collected, and meanwhile, the water from a boundary region is supplemented to the condensing section of the comprehensive tower for maintaining the water balance of the system;
the cooling capacity required by the circulating liquid cooler is provided by an absorption heat pump, the temperature of cooling water generated by the absorption heat pump is 10-30 ℃, the cooling water is subjected to heat exchange to 20-40 ℃ by the circulating liquid cooler, and the cooling water is pressurized to 0.1-1.0 Mpag by a cooling water pressurizing pump and then returned to the absorption heat pump for circulation cooling;
the air from the environment at normal temperature and normal pressure is pressurized by a fan, is heated to 60-90 ℃ by an air preheater, is sent to the air heater to be heated to 80-150 ℃, and is sent to a flue gas discharge port to be mixed with condensed flue gas;
the heat required by the air preheater is provided by an absorption heat pump, the temperature of heat medium water generated by the absorption heat pump is 70-95 ℃, and the heat is exchanged to 55-75 ℃ by the air preheater and then returned to the absorption heat pump for cyclic heating;
the low-pressure steam from the boundary region has the temperature of 130-150 ℃ and the pressure of 0.1-0.6 Mpa, and is divided into two parts, one part is sent to an air heater to be used as a heating source, and the other part is sent to the absorption heat pump to be used as driving heat, and the generated condensate is sent out of the boundary region;
the absorption heat pump uses low-pressure steam as a driving source, low-temperature heat energy in circulating absorption liquid of a condensing section is transferred into heat medium water, the temperature of the heat medium water is 70-95 ℃, the heat medium water is pressurized to 0.1-1.0 Mpa by a heat medium water pressurizing pump and then divided into two parts, the first part is sent to an air heater for heating air, and the second part is sent out of a boundary area for use;
the mass flow ratio of the first stream of heat medium water to the second stream of heat medium water is 1:9-1:2;
the ratio of the heat added by the heat medium water generated by the absorption heat pump to the heat of the circulating absorption liquid removed by the circulating cooler is 1.5:1-2.5:1.
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| EP1174172A3 (en) * | 2000-07-19 | 2003-02-05 | Emil A.J. D.I. Wieser-Linhart | Process and installation for gas purification |
| CN105214457B (en) * | 2014-06-05 | 2018-04-17 | 魏雄辉 | A kind of fume desulfuring and denitrifying Processes and apparatus |
| CN209034090U (en) * | 2018-08-29 | 2019-06-28 | 航天环境工程有限公司 | A kind of ammonia process of desulfurization flue gas disappears white waste heat depth recovery system |
| CN109045976A (en) * | 2018-08-29 | 2018-12-21 | 航天环境工程有限公司 | A kind of ammonia process of desulfurization flue gas disappears white waste heat depth recovery system and application |
| CN109737446A (en) * | 2019-01-06 | 2019-05-10 | 大唐(北京)能源管理有限公司 | A kind of recycling of power plant boiler smoke discharging residual heat and flue gas disappear white system |
| CN109772071A (en) * | 2019-03-21 | 2019-05-21 | 上海电力学院 | White plume based on upper spray upper air spray column eliminates system |
| CN210612932U (en) * | 2019-09-11 | 2020-05-26 | 广州市天赐三和环保工程有限公司 | White smoke eliminating device for smoke spraying, heat exchange, condensation and waste heat recovery |
| CN112221286A (en) * | 2020-09-08 | 2021-01-15 | 中石化宁波工程有限公司 | Deep absorption tower for flue gas treatment, flue gas treatment system and process |
| CN215294975U (en) * | 2020-11-02 | 2021-12-24 | 华北电力大学 | Flue gas waste heat recovery and white smoke elimination integrated system based on absorption heat pump |
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