CN114392639A - 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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- CN114392639A CN114392639A CN202111640268.8A CN202111640268A CN114392639A CN 114392639 A CN114392639 A CN 114392639A CN 202111640268 A CN202111640268 A CN 202111640268A CN 114392639 A CN114392639 A CN 114392639A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- 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
- B01D53/18—Absorbing units; Liquid distributors therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/06—Spray cleaning
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- 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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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- 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
- B01D53/1406—Multiple stage absorption
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- F24—HEATING; RANGES; VENTILATING
- F24H—FLUID HEATERS, e.g. WATER OR AIR HEATERS, HAVING HEAT-GENERATING MEANS, e.g. HEAT PUMPS, IN GENERAL
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Abstract
The invention relates to a catalytic cracking flue gas waste heat utilization coupling desulfurization wet smoke and rain elimination process, which not only can effectively utilize the flue gas waste heat, but also can reduce the energy consumption in the catalytic cracking wet smoke and rain elimination process. The main embodiment is as follows: the flue gas is condensed without an additional cold source, so that the system consumption is reduced; the absorption heat pump is adopted, so that the 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 absorption heat pump is utilized to convert the low-temperature heat in the desulfurization circulating liquid into medium-high temperature heat in the heating medium water, so that the quality of the heat is improved, and the availability of the heat is further enhanced; the flue gas condensation setting greatly reduces the consumption of system make-up water.
Description
Technical Field
The invention 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 rain elimination process.
Background
In recent years, along with the development of environmental problems, the nation pays more attention to environmental protection problems, and the emission standard of atmospheric pollution areas 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 of the emission of atmospheric pollutants, wherein the flue gas discharged by the regenerator of the catalytic cracking unit 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 processes, and the carbon deposit on the catalyst needs to be regenerated and burnt out in a regenerator, so that the activity of the catalyst is recovered. The carbon deposit is burnt out by using air through a regenerator, the entrained catalyst is separated from the regenerated flue gas through a cyclone separator, the regenerated flue gas is exhausted after energy is recovered through a smoke machine and a waste heat boiler, and the catalytic cracking regenerated flue gas is generated in the process. The regenerated flue gas from catalytic cracking has the characteristics of wide fluctuation range of sulfur content, large particle size range of particles, high content of particles below submicron level and the like.
In the prior art, a wet removal process is generally adopted for purification treatment of catalytic cracking regenerated flue gas, and the regenerated flue gas is washed by a large amount of circulating absorption liquid to remove particles and sulfides in the regenerated flue gas and then is discharged into the atmosphere. Because the wet-method removal process is adopted, the exhausted flue gas is saturated flue gas and carries certain water vapor, and the wet flue gas is contacted with ambient air to reduce the temperature in the discharging process, so that obvious white smoke and even rain fall are formed, and the surrounding environment is influenced.
Meanwhile, in the purification process of catalytic cracking regenerated flue gas, the residual heat of the flue gas is discharged through the flue gas, and the circulating absorption liquid also absorbs the residual heat of the flue gas, at present, the residual heat of wet flue gas and circulating slurry is generally not utilized or is not fully utilized, for example, the utility model discloses a wet smoke rain flue heat exchange white smoke elimination and condensate water recovery device which is applied to the utility model with the application number of CN201721593098.1, the white smoke elimination adopts the mode of firstly condensing and then heating, the flue gas condensing adopts circulating water, the flue gas is heated again by steam, although the elimination of wet smoke rain can be realized, the energy consumption is high, the operating cost is expensive, and the application of the technology is limited.
Disclosure of Invention
The invention aims to solve the technical problem of providing a process for improving the utilization efficiency of the catalytic cracking flue gas waste heat and coupling desulfurization wet smoke and rain elimination, aiming at the current situation of the prior art, wherein the process not only can effectively utilize the flue gas waste heat, but also can reduce the energy consumption in the catalytic cracking wet smoke and rain elimination process.
The technical scheme adopted by the invention for solving the technical problems is as follows:
a wet flue gas rain elimination process for coupling catalytic cracking flue gas waste heat utilization and desulfurization comprises the following steps:
the temperature of catalytic cracking regeneration flue gas sent from a battery compartment is 130-300 ℃, the pressure is 0.002-0.01 Mpag, the flue gas is subjected to first-stage washing absorption of a main absorption tower and second-stage washing absorption of an integrated tower to remove sulfides and particles in the flue gas, then the flue gas is sent to a demister to remove free water in the flue gas, the temperature of the flue gas is reduced to 50-80 ℃, and the flue gas is sent to a condensation section of the integrated tower;
the comprehensive tower condensation section is provided with a circulating pump and a circulating liquid cooler, circulating liquid in the comprehensive tower condensation section is pressurized to 0.3-1.0 Mpag through the circulating pump, the circulating liquid is sent to the circulating cooler to be cooled to 35-55 ℃, then the circulating liquid is sent to the comprehensive tower condensation section to be directly sprayed and contacted with flue gas, the flue gas is cooled to 37-62 ℃, the flue gas is mixed with hot air from an air heater after being removed and condensed by a secondary demister to generate condensed water, the temperature of the mixed flue gas is 50-85 ℃, the mixed flue gas is discharged to the atmosphere, the treatment and the discharge of the wet smoke rain are realized, the sprayed circulating liquid is collected and then sent to the circulating pump for continuous utilization, and meanwhile, supplementing water from a boundary area is sent to the comprehensive tower condensation section to maintain the water balance of the system;
the cooling capacity required by the circulating liquid cooler is provided by an absorption heat pump, the absorption heat pump generates cooling water with the temperature of 10-30 ℃, the cooling water is subjected to heat exchange to 20-40 ℃ through the circulating liquid cooler, and the cooling water is pressurized to 0.1-1.0 Mpag through a cooling water pressurizing pump and then returns to the absorption heat pump for circulating cooling;
after being pressurized by a fan, normal-temperature and normal-pressure air from the environment is heated to 60-90 ℃ by an air preheater, then is sent to an air heater to be heated to 80-150 ℃, and then 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 hot medium water generated by the absorption heat pump is 70-95 ℃, and the hot medium water is returned to the absorption heat pump for circulation heating after being subjected to heat exchange to 55-75 ℃ by the air preheater.
Preferably, the temperature of low-pressure steam from the battery limits is 130-200 ℃, the pressure is 0.3-1.0 Mpag, the low-pressure steam is divided into two streams, one stream is sent to an air heater to be used as a heating heat source, the other stream is sent to the absorption heat pump to be used as driving heat, and the generated condensate is sent out of the battery limits; the absorption heat pump uses low-pressure steam as a driving source, transfers low-temperature heat energy in the circulating absorption liquid of the condensation section to heat medium water, generates 70-95 ℃ of the temperature of the heat medium water, is pressurized to 0.1-1.0 Mpag by a heat medium water pressurizing pump and then is divided into two strands, one strand is sent to an air heater for heating air, the other strand is sent out of a boundary area for utilization, and the mass flow rate ratio of the two strands 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 to transfer low-temperature heat energy in the circulating absorption liquid into heat medium water, so that a large amount of middle-temperature useful heat energy is generated, namely, the absorption heat pump is driven by a small amount of high-temperature heat energy to increase the heat energy of a large amount of low-temperature heat sources to middle temperature, so that the utilization efficiency of the heat energy is improved, and the utilization rate of the heat energy 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, hot water with the temperature of more than 90 ℃ can be used as a driving heat source of the absorption heat pump.
Compared with the prior art, the invention has the following advantages:
1. the flue gas is condensed without an additional cold source, so that the system consumption is reduced;
2. the absorption heat pump is adopted, so that the 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 absorption heat pump is utilized to convert the low-temperature heat in the desulfurization circulating liquid into medium-high temperature heat in the heating medium water, so that the quality of the heat is improved, and the availability of the heat is further enhanced;
4. the flue gas condensation setting greatly reduces the consumption of system make-up water.
Drawings
FIG. 1 is a process flow diagram of example 1 of the present invention;
FIG. 2 is a process flow diagram of example 2 of the present invention.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
Example 1:
as shown in fig. 1, the catalytic cracking flue gas waste heat utilization coupling desulfurization wet flue gas rain elimination process of the embodiment includes the following steps:
the temperature of the catalytic cracking regeneration flue gas sent from a battery compartment is 180 ℃, the pressure is 0.005Mpag, the flue gas is sent to a first-stage demister 12 to remove free water in the flue gas after being washed and absorbed by a first section of a main absorption tower 2 and a second section 11 of an integrated tower to remove sulfides and particulate matters in the flue gas, and the temperature of the flue gas is reduced to 55 ℃, and the flue gas is sent to a condensation section 13 of the integrated 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 by the circulating pump 5, the circulating liquid is sent to the circulating cooler 6 to be cooled to 48 ℃, then the circulating liquid is sent to the comprehensive tower condensation section 13 to be directly sprayed and contacted with flue gas, the flue gas is cooled to 50 ℃, the flue gas is mixed with hot air from an air heater 10 after being removed and condensed by a secondary demister 14 to generate condensed water, the mixed flue gas is discharged to the atmosphere at the temperature of 75 ℃ below zero, the treatment and the discharge of wet smoke rain are realized, the sprayed circulating liquid is collected and then sent to the circulating pump 5 for continuous utilization, and meanwhile, make-up water from a boundary area is sent to the comprehensive tower condensation section 13 for maintaining the balance of water of the system;
the cooling capacity required by the circulating liquid cooler 6 is provided by the absorption heat pump 7, the absorption heat pump 7 generates cooling water with the temperature of 20 ℃, the cooling water is subjected to heat exchange to 30 ℃ through the circulating liquid cooler 6, and the cooling water is pressurized to 0.6Mpag through the cooling water pressure pump 11 and then returns to the absorption heat pump 7 for circulation cooling;
the normal temperature and normal pressure air from the environment is pressurized by a fan 8, heated by an air preheater 9 at 70 ℃, sent to an air heater 10 to be heated to 120 ℃, and then sent to a smoke discharge port to be mixed with the condensed smoke.
In the 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 85 ℃, and the heat medium water returns to the absorption heat pump for circulating heating after being subjected to heat exchange to 60 ℃ by the air preheater 9.
In the embodiment, the low-pressure steam from the battery compartment has the temperature of 150 ℃ and the pressure of 0.6Mpag, and is divided into two streams, one stream is sent to an air heater 10 to be used as a heating heat source, the other stream is sent to an absorption heat pump 7 to be used as driving heat, and the generated condensate is sent out of the battery compartment; the absorption heat pump 7 uses low-pressure steam as a driving source to transfer low-temperature heat energy in the circulating absorption liquid in the condensation section to heat medium water, the temperature of the generated heat medium water is 85 ℃, the heat medium water is pressurized to 0.6Mpag by a heat medium water pressurizing pump 12 and then is divided into two parts, one part is sent to an air heater 10 to be used for heating air, the other part is sent out of a boundary area to be used, and the mass flow ratio of the two parts of the heat medium water is 1: 2.
The ratio of the heat quantity added by the heat medium water generated by the absorption heat pump 7 to the heat quantity of the circulating absorption liquid removed by the circulating cooler 6 is 1.5: 1.
The absorption heat pump 7 transfers low-temperature heat energy in the circulating absorption liquid to heat medium water by using a small amount of high-temperature steam as a driving heat source, so that a large amount of middle-temperature useful heat energy is generated. The circulating cooler 6 for condensing the flue gas adopts cooling water generated by the absorption heat pump 7, thereby avoiding the consumption of an additional cold source and further reducing the consumption.
Example 2:
as shown in fig. 2, the catalytic cracking flue gas waste heat utilization coupling desulfurization wet flue gas rain elimination process of the embodiment includes the following steps:
the temperature of catalytic cracking regeneration flue gas sent from a battery compartment is 260 ℃, the pressure is 0.004Mpag, the flue gas is washed and absorbed by a first section of a main absorption tower 2 to remove sulfide and particulate matters in the flue gas, then the flue gas is sent to a first-stage demister 12 to remove free water in the flue gas, the temperature of the flue gas is reduced to 62 ℃, and the flue gas is sent to a condensation 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 by the circulating pump 5, the circulating liquid is sent to the circulating cooler 6 to be cooled to 55 ℃, then the circulating liquid is sent to the comprehensive tower condensation section 13 to be directly sprayed and contacted with flue gas, the flue gas is cooled to 57 ℃, the flue gas is mixed with hot air from an air heater 10 after being removed and condensed by a secondary demister 14 to generate condensed water, the mixed flue gas is discharged to the atmosphere at the temperature of 80 ℃, the treatment and discharge of wet smoke rain are realized, the sprayed circulating liquid is collected and then sent to the circulating pump 5 for continuous utilization, and meanwhile, make-up water from a boundary area is sent to the comprehensive tower condensation section 13 to maintain 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 absorption heat pump 7 generates cooling water with the temperature of 30 ℃, the cooling water is subjected to heat exchange to 40 ℃ through the circulating liquid cooler 6, and the cooling water is pressurized to 1.0Mpag through the cooling water pressure pump 11 and then returns to the absorption heat pump 7 for circulation cooling;
the normal temperature and normal pressure air from the environment is pressurized by a fan 8, heated by an air preheater 9 at 85 ℃, sent to an air heater 10 to be heated to 120 ℃, and then sent to a smoke discharge port to be mixed with the condensed smoke.
In the 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 medium water returns to the absorption heat pump for circulation heating after being subjected to heat exchange to 75 ℃ by the air preheater 9.
In the embodiment, the temperature of hot water from a boundary area is 130 ℃, the pressure is 1.0Mpag, the hot water is divided into two streams, one stream is sent to an air heater 10 to be used as a heating heat source, the other stream is sent to an absorption heat pump 7 to be used as driving heat, and the driving heat return water temperature of the absorption heat pump 7 is 80 ℃ and is sent out of the boundary area; the absorption heat pump 7 uses hot water as a driving source, transfers low-temperature heat energy in the circulating absorption liquid of the condensation section to heat medium water, generates the temperature of the heat medium water of 95 ℃, is pressurized to 1.0Mpag by a heat medium water pressurizing pump 12 and then is divided into two parts, one part is sent to an air heater 10 for heating air, the other part is sent out of a boundary area for utilization, and the mass flow ratio of the two parts of the heat medium water is 1: 5.
The ratio of the heat quantity added by the heat medium water generated by the absorption heat pump 7 to the heat quantity of the circulating absorption liquid removed by the circulating cooler 6 is 2: 1.
The absorption heat pump 7 transfers low-temperature heat energy in the circulating absorption liquid to heat medium water by using a small amount of high-temperature steam as a driving heat source, so that a large amount of middle-temperature useful heat energy is generated. The circulating cooler 6 for condensing the flue gas adopts cooling water generated by the absorption heat pump 7, thereby avoiding the consumption of an additional cold source and further reducing the consumption.
Claims (6)
1. A wet flue gas rain elimination process for coupling catalytic cracking flue gas waste heat utilization and desulfurization is characterized by comprising the following steps:
the temperature of catalytic cracking regeneration flue gas sent from a battery compartment is 130-300 ℃, the pressure is 0.002-0.01 Mpag, the flue gas is subjected to first-stage washing absorption in a main absorption tower (2) and second-stage washing absorption in an integrated tower (11) to remove sulfide and particulate matters in the flue gas, then the flue gas is sent to a first-stage demister (12) to remove free water in the flue gas, the temperature of the flue gas is reduced to 50-80 ℃, and the flue gas is sent to a condensation section (13) of the integrated 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 0.1-1.0 Mpag through the circulating pump (5), sent to the circulating cooler (6) to be cooled to 35-55 ℃, then sent to the comprehensive tower condensation section (13) to be directly sprayed and contacted with flue gas, the flue gas is cooled to 37-62 ℃, the flue gas is subjected to condensation removal through a secondary demister (14) to generate condensed water and then mixed with hot air from an air heater (10), the temperature of the mixed flue gas is 50-85 ℃ and is discharged to the atmosphere, the treatment and discharge of wet smoke and rain are realized, the sprayed circulating liquid is collected and then sent to the circulating pump (5) for continuous utilization, and meanwhile, the supplementing water from a boundary area is sent to the comprehensive tower condensation section (13) to maintain 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 absorption heat pump (7) generates cooling water with the temperature of 10-30 ℃, the cooling water is subjected to heat exchange to 20-40 ℃ through the circulating liquid cooler (6), and the cooling water is pressurized to 0.1-1.0 Mpag through the cooling water pressurizing pump (11) and then returns to the absorption heat pump (7) for circulating cooling;
air from the environment at normal temperature and normal pressure is pressurized by a fan (8), heated by an air preheater (9) at 60-90 ℃, sent to an air heater (10) and heated to 80-150 ℃, and then sent to a flue gas discharge port to be mixed with condensed flue gas.
2. The catalytic cracking flue gas waste heat utilization coupling desulfurization wet flue gas rain elimination process according to claim 1, characterized in that: the heat required by the air preheater (9) is provided by the absorption heat pump (7), the temperature of the hot medium water generated by the absorption heat pump (7) is 70-95 ℃, and the hot medium water is returned to the absorption heat pump for circulating heating after being subjected to heat exchange to 55-75 ℃ by the air preheater (9).
3. The catalytic cracking flue gas waste heat utilization coupling desulfurization wet flue gas rain elimination process according to claim 1, characterized in that: the temperature of low-pressure steam from a boundary area is 130-150 ℃, the pressure is 0.1-0.6 Mpag, the low-pressure steam is divided into two streams, one stream is sent to an air heater (10) to be used as a heating heat source, the other stream is sent to the absorption heat pump (7) to be used as driving heat, and generated condensate is sent out of the boundary area.
4. The catalytic cracking flue gas waste heat utilization coupling desulfurization wet flue gas and rain elimination process according to claim 3, characterized in that: the absorption heat pump (7) uses low-pressure steam as a driving source, transfers low-temperature heat energy in the circulating absorption liquid of the condensation section to heat medium water, generates heat medium water with the temperature of 70-95 ℃, is pressurized to 0.1-1.0 Mpag by a heat medium water pressurizing pump (12) and then is divided into two strands, wherein the first strand is sent to an air heater (10) for heating air, and the second strand is sent out of a boundary area for utilization.
5. The catalytic cracking flue gas waste heat utilization coupling desulfurization wet flue gas and rain elimination process according to claim 4, characterized in that: 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.
6. The catalytic cracking flue gas waste heat utilization coupling desulfurization wet flue gas rain elimination process according to claim 1, characterized in that: 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: 1-2.5: 1.
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| CN114392639B (en) | 2023-07-14 |
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