CN116351224A - Sodium alkali desulfurization process for catalytic cracking regenerated flue gas - Google Patents

Sodium alkali desulfurization process for catalytic cracking regenerated flue gas Download PDF

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Publication number
CN116351224A
CN116351224A CN202310036593.6A CN202310036593A CN116351224A CN 116351224 A CN116351224 A CN 116351224A CN 202310036593 A CN202310036593 A CN 202310036593A CN 116351224 A CN116351224 A CN 116351224A
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absorption tower
flue gas
section
circulating liquid
catalytic cracking
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CN202310036593.6A
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Chinese (zh)
Inventor
唐永超
程彬彬
卢新军
孙蓓蓓
柳杨
孙晓怡
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Sinopec Engineering Group Co Ltd
Sinopec Ningbo Engineering Co Ltd
Sinopec Ningbo Technology Research Institute
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Sinopec Engineering Group Co Ltd
Sinopec Ningbo Engineering Co Ltd
Sinopec Ningbo Technology Research Institute
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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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/346—Controlling the process
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/304—Alkali metal compounds of sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/604—Hydroxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases

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  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)

Abstract

The utility model relates to a catalytic cracking regenerated flue gas sodium alkali desulfurization process, which utilizes waste heat of catalytic cracking regenerated flue gas to carry out secondary concentration on an externally discharged circulating liquid in an absorption tower, thereby greatly reducing the externally discharged brine content generated by desulfurization; the concentrated desulfurized salt-containing water is sent to the catalytic cracking regenerated flue gas for spraying and mixing, so that the desulfurized salt-containing water is eliminated, and excessive heat waste is avoided; the spraying of the desulfurization salt-containing water promotes the viscosity agglomeration of small particles in the flue gas and improves the dust removal effect; the particulate matters in the flue gas are removed, so that the scaling phenomenon in the absorption tower is improved, and the long-period operation of the desulfurization system is ensured; the utility model greatly reduces the water supplement of the desulfurization system and reduces the consumption.

Description

Sodium alkali desulfurization process for catalytic cracking regenerated flue gas
Technical Field
The utility model relates to the field of catalytic cracking regeneration flue gas purification, in particular to a sodium-alkali desulfurization process for catalytic cracking regeneration flue gas.
Background
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. Carbon deposition can be generated on the surface of the catalyst in the catalytic cracking and catalytic cracking reaction process, and the catalyst needs to enter a regenerator for regeneration to restore the activity. The air is used to enter a regenerator to burn off carbon deposition, the generated flue gas is separated from entrained catalyst by a cyclone separator, and the flue gas is exhausted after energy is recovered by a flue gas machine and a waste heat boiler, so that catalytic cracking regenerated flue gas is generated in the process.
In the prior art, aiming at catalytic cracking regeneration flue gas purification treatment, a wet sodium-alkali method 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. However, in order to avoid the enrichment of particulate matters and salts in the absorption tower and avoid the generation of a large amount of wastewater containing particulate matters and salts, water treatment equipment is additionally arranged, and the problem of salt wastewater discharge exists.
For example, the utility model patent with publication number CN201871320U discloses a desulfurization and dust removal device for catalytic cracking regeneration flue gas, which uses alkali liquor to absorb and neutralize sulfides in the catalytic cracking regeneration flue gas, and circularly washes and removes particulates in the catalytic cracking regeneration flue gas, in order to keep the balance of salt and particulates in the tower, the slurry at the bottom of the absorption tower discharges a large amount of sewage to a water treatment unit through a discharge pump, so that particulates and COD in the sewage can be further removed, and a large amount of salt-containing wastewater discharge is still generated.
Disclosure of Invention
Aiming at the current state of the art, the utility model provides a catalytic cracking regenerated flue gas sodium alkali desulfurization process capable of avoiding the discharge of salt-containing wastewater.
The technical scheme adopted for solving the technical problems is as follows:
a catalytic cracking regeneration flue gas sodium alkali desulfurization process comprises the following steps:
the temperature of regenerated flue gas after SCR denitration from catalytic cracking is 320-400 ℃, the pressure is 0.005-0.02 Mpag, and SO 2 The content is 500-3000 mg/Nm 3 The content of the particles is 100-1000 mg/Nm 3 Dividing into two streams, wherein one stream is subjected to heat recovery through a catalytic cracking waste heat boiler low-temperature economizer and is cooled to 150-260 ℃; the second strand is sprayed, mixed and cooled to 150-260 ℃ by high-salt water content, and is mixed into the first strand of regenerated flue gas after heat recovery and then is sent to a dust remover;
the content of particles in the regenerated flue gas discharged from the dust remover is reduced to 0-20 mg/Nm 3 Sending to the lower section of the absorption tower;
in the lower section of the absorption tower, the regenerated flue gas is fully and reversely contacted with circulating liquid in the lower section of the absorption tower, cooled to 50-65 ℃ by chilling, and sent to the middle section of the absorption tower; the lower circulation liquid of the absorption tower is gasified and concentrated by the flue gas, the salt content is increased to 6-16 wt%, the lower circulation liquid is pressurized to 0.2-0.6 Mpag by a lower circulation liquid pump and then divided into two parts, the first part is sent to a lower spray pipe of the absorption tower, the regenerated flue gas entering the absorption tower is chilled and washed after being atomized by a nozzle, the second part is sent to a buffer tank for decompression to 0.01-0.1 Mpag, the gas phase is returned to the absorption tower after decompression, the liquid phase is pressurized to 0.2-0.6 Mpag by a pump and is fully fluidized by compressed air, and then sent to the second part for catalytic cracking SCR denitration and then the regenerated flue gas is sprayed and mixed;
in the middle section of the absorption tower, the regenerated flue gas is fully contacted with the middle section circulating liquid added with alkali liquor to remove SO in the flue gas 2 Removing entrainment in wet flue gas by a demister, and then delivering the entrainment to the upper section of an absorption tower; the temperature of the middle circulating liquid discharged from the bottom of the middle section of the absorption tower is 50-65 ℃, the temperature is pressurized to 0.3-0.7 Mpa by a middle circulating liquid pump and then divided into two streams, the first stream is sent to a middle spraying pipe of the absorption tower, the regenerated flue gas entering the absorption tower is washed and absorbed after being atomized by a nozzle, and the second stream is sent to the lower section of the absorption tower to maintain the water balance of the lower section of the absorption tower;
in the upper section of the absorption tower, the wet flue gas is fully contacted with the circulating liquid in the upper section, SO that the residual SO in the flue gas is further removed 2 And salt components in entrainment, and further removing fog drops in the flue gas through a high-efficiency demister, and then discharging the fog drops to the atmosphere; the temperature of the upper circulating liquid discharged from the bottom of the upper section of the absorption tower is 50-65 ℃, the upper circulating liquid is pressurized to 0.4-0.8 Mpag by an upper circulating liquid pump and then is sent to a spray pipe of the upper section of the absorption tower, and the wet flue gas is subjected to secondary washing absorption after being atomized by a nozzle.
Preferably, the flow ratio of the first strand of regeneration flue gas to the second strand of regeneration flue gas is 4:1-19:1.
Preferably, the flow rate of the second lower-stage circulating liquid is controlled, and the salt content in the lower-stage circulating liquid is maintained to be 6-16 wt%.
Preferably, the flow rate of the second middle circulating liquid is controlled, and the salt content in the middle circulating liquid is maintained to be 3-8 wt%.
Preferably, a first partition plate and a second partition plate which are vertically arranged at intervals are arranged in the absorption tower, the first partition plate and the second partition plate divide the absorption tower into an upper absorption tower section, a middle absorption tower section and a lower absorption tower section, a first riser pipe which is vertically arranged and vertically penetrated is arranged on the first partition plate, the upper end of the first riser pipe is positioned above the liquid level of the upper absorption tower section, a second riser pipe which is vertically arranged and vertically penetrated is arranged on the second partition plate, and the upper end of the second riser pipe is positioned above the liquid level of the middle absorption tower section;
the upper section of the absorption tower is provided with high-efficiency demisters and upper-section spray pipes which are arranged at intervals from top to bottom; the middle section of the absorption tower is provided with foam removers and middle section spray pipes which are arranged at intervals from top to bottom; the lower section of the absorption tower is internally provided with lower section spray pipes and smoke distributors which are arranged at intervals from top to bottom; the inlet of the regeneration flue gas is located at the side wall of the absorber tower and is arranged below the smoke distributor.
Preferably, a middle section circulating liquid pump is arranged at the side of the absorption tower, an inlet of the middle section circulating liquid pump is connected with the bottom of the middle section of the absorption tower, an outlet of the middle section circulating liquid pump is connected with a middle section spray pipe through a first pipeline, is connected with the lower section of the absorption tower through a second pipeline, and the connecting position is located below the liquid level.
Preferably, an upper circulation liquid pump is arranged beside the absorption tower, an inlet of the upper circulation liquid pump is connected with the bottom of the upper section of the absorption tower, and an outlet of the upper circulation liquid pump is connected with the upper spray pipe through a third pipeline.
Preferably, the utility model further comprises a buffer tank, a lower circulation liquid pump is arranged at the side of the absorption tower, an inlet of the lower circulation liquid pump is connected with the bottom of the lower section of the absorption tower, and an outlet of the lower circulation liquid pump is connected with a lower spray pipe through a fourth pipeline and is connected with the buffer tank through a fifth pipeline.
Preferably, the bottom of the buffer tank is fully fluidized by compressed air through a sixth pipeline and a booster pump, and then sent to be mixed with regenerated flue gas after denitration of the second catalytic cracking SCR.
Compared with the prior art, the utility model has the advantages that: the utility model utilizes the waste heat of the catalytic cracking regenerated flue gas to carry out secondary concentration on the discharged circulating liquid in the absorption tower, thereby greatly reducing the discharged brine content generated by desulfurization; the concentrated desulfurized salt-containing water is sent to the catalytic cracking regenerated flue gas for spraying and mixing, so that the desulfurized salt-containing water is eliminated, and excessive heat waste is avoided; the spraying of the desulfurization salt-containing water promotes the viscosity agglomeration of small particles in the flue gas and improves the dust removal effect; the particulate matters in the flue gas are removed, so that the scaling phenomenon in the absorption tower is improved, and the long-period operation of the desulfurization system is ensured; the utility model greatly reduces the water supplement of the desulfurization system and reduces the consumption.
Drawings
FIG. 1 is a process flow diagram of an embodiment of the present utility model.
Detailed Description
The utility model is described in further detail below with reference to the embodiments of the drawings.
As shown in fig. 1, the catalytic cracking flue gas desulfurization process of the present embodiment includes the steps of:
the temperature of regenerated flue gas after SCR denitration from catalytic cracking is 320 ℃, the pressure is 0.01Mpag and SO 2 At a concentration of about 800mg/Nm 3 The particle content was 200mg/Nm 3 Dividing into two streams, wherein one stream is subjected to heat recovery through a catalytic cracking waste heat boiler low-temperature economizer 1 and is cooled to 170 ℃; the second strand is sprayed with high-salt water, mixed and cooled to 170 ℃, and then is gathered into the first strand of regenerated flue gas after heat recovery and is sent to a dust remover 2; the flow ratio of the first stream of regenerated flue gas to the second stream of regenerated flue gas is 5:1; the content of the particles in the regenerated flue gas discharged from the dust remover 2 is reduced to 10mg/Nm 3 Is sent to the lower section of the absorption tower 3;
in the lower section of the absorption tower 3, the regenerated flue gas is fully and reversely contacted with circulating liquid in the lower section of the absorption tower, cooled to 55 ℃ by chilling, and sent to the middle section of the absorption tower 3 through the air rising hole 32. The circulating liquid at the lower section of the absorption tower is gasified and concentrated by the flue gas, the salt content is increased to 10wt%, the circulating liquid is pressurized to 0.5Mpa by a circulating liquid pump at the lower section 6 and divided into two streams, the first stream is sent to a spraying pipe 31 at the lower section of the absorption tower, the regenerated flue gas entering the absorption tower is chilled and washed after being atomized by a nozzle, the circulating liquid at the second lower section is sent to a buffer tank 7 for decompression to 0.01-0.1 Mpa, the gas phase returns to the absorption tower after decompression, the liquid phase is pressurized to 0.2-0.6 Mpa by the pump and is fully fluidized by compressed air at 0.7Mpa, and then the liquid phase is sent to the regenerated flue gas for spraying and mixing after the denitration of the second catalytic cracking SCR; controlling the flow of the second lower circulation liquid, and maintaining the salt content in the lower circulation liquid to be 10wt%;
in the middle section of the absorption tower 3, the regenerated flue gas is fully contacted with the middle section circulating liquid added with alkali liquor to remove SO in the flue gas 2 Removing entrainment in wet flue gas by a demister 34, and delivering to a suction port 35The upper section of the tower 3. The temperature of the middle circulating liquid discharged from the bottom of the middle section of the absorption tower 3 is 55 ℃, the temperature is pressurized to 0.5Mpag by the middle circulating liquid pump 4 and then divided into two parts, the first part is sent to the middle section spray pipe 33 of the absorption tower, the regenerated flue gas entering the absorption tower is washed and absorbed after being atomized by a nozzle, and the second part is sent to the lower section of the absorption tower 3 to maintain the water balance of the lower section of the absorption tower; controlling the flow of the second middle circulating liquid, and maintaining the salt content in the middle circulating liquid to be 5wt%;
in the upper section of the absorption tower 3, the wet flue gas is fully contacted with the circulating liquid in the upper section, SO that the residual SO in the flue gas is further removed 2 And salt components in entrainment, and further removing the entrainment of droplets in the flue gas by a high-efficiency demister 37, and then discharging the flue gas to the atmosphere; the temperature of the upper circulating liquid discharged from the bottom of the upper section of the absorption tower 3 is 55 ℃, the upper circulating liquid is pressurized to 0.6Mpa by the upper circulating liquid pump 5 and then is sent to the upper spraying pipe 36 of the absorption tower, and the wet flue gas is subjected to secondary washing absorption after being atomized by a nozzle.
In this embodiment, a first partition board and a second partition board are disposed in the absorption tower 3 at intervals from top to bottom, the first partition board and the second partition board divide the absorption tower 3 into an upper section of the absorption tower, a middle section of the absorption tower and a lower section of the absorption tower, a first riser 35 is disposed on the first partition board, the upper end of the first riser 35 is located above the liquid level of the upper section of the absorption tower 3, a second riser 32 is disposed on the second partition board, the upper end of the second riser 32 is located above the liquid level of the middle section of the absorption tower 3; the upper section of the absorption tower 3 is provided with high-efficiency demisters 37 and upper-section spray pipes 36 which are arranged at intervals from top to bottom; the middle section of the absorption tower 3 is provided with foam removers 34 and middle section spray pipes 33 which are arranged from top to bottom at intervals; the lower section of the absorption tower 3 is provided with lower section spray pipes 31 and smoke distributors 30 which are arranged at intervals from top to bottom; the inlet for the regeneration flue gas is located in the side wall of the absorber tower 3 and is arranged below the smoke distributor 30.
The side of the absorption tower 3 is provided with a middle circulating liquid pump 4, the inlet of the middle circulating liquid pump 4 is connected with the bottom of the middle section of the absorption tower 3, the outlet of the middle circulating liquid pump 4 is connected with a middle spraying pipe 33 through a first pipeline, and is connected with the lower section of the absorption tower 3 through a second pipeline, and the joint is positioned below the liquid level. An upper circulation liquid pump 5 is arranged beside the absorption tower 3, an inlet of the upper circulation liquid pump 5 is connected with the bottom of the upper section of the absorption tower 3, and an outlet of the upper circulation liquid pump 5 is connected with an upper spray pipe 36 through a third pipeline.
The embodiment is also provided with a buffer tank 7, a lower circulation liquid pump 6 is arranged beside the absorption tower 3, an inlet of the lower circulation liquid pump 6 is connected with the bottom of the lower section of the absorption tower 3, and an outlet of the lower circulation liquid pump 6 is connected with a lower spray pipe 31 through a fourth pipeline and is connected with the buffer tank 7 through a fifth pipeline. The bottom of the buffer tank 7 is fully fluidized by compressed air through a sixth pipeline and a booster pump 8, and then is sent to be mixed with regenerated flue gas after the denitration of the second catalytic cracking SCR.
Taking a 300 ten thousand ton/year catalytic cracker as an example, it produces about 440000Nm of regenerated flue gas 3 /h，SO 2 At a concentration of about 780mg/Nm 3 The particle content was about 230mg/Nm 3 The main parameters of the conventional sodium-alkali wet desulfurization technology are compared under the reference and are shown in table 1.
TABLE 1
Figure BDA0004048952160000041
Figure BDA0004048952160000051

Claims (9)

1. A catalytic cracking regeneration flue gas sodium alkali desulfurization process is characterized by comprising the following steps:
the temperature of regenerated flue gas after SCR denitration from catalytic cracking is 320-400 ℃, the pressure is 0.005-0.02 Mpag, and SO 2 The content is 500-3000 mg/Nm 3 The content of the particles is 100-1000 mg/Nm 3 Dividing into two streams, wherein one stream is subjected to heat recovery through a catalytic cracking waste heat boiler low-temperature economizer and is cooled to 150-260 ℃; the second strand is sprayed, mixed and cooled to 150-260 ℃ by high-salt water content, and then is gathered into the first strand for regeneration after heat recoveryAfter the flue gas is in the flue gas, the flue gas is sent to a dust remover;
the content of particles in the regenerated flue gas discharged from the dust remover is reduced to 0-20 mg/Nm 3 Sending to the lower section of the absorption tower;
in the lower section of the absorption tower, the regenerated flue gas is fully and reversely contacted with circulating liquid in the lower section of the absorption tower, cooled to 50-65 ℃ by chilling, and sent to the middle section of the absorption tower; the circulating liquid at the lower section of the absorption tower is gasified and concentrated by the flue gas, the salt content is increased to 6-16 wt%, the circulating liquid at the lower section is pressurized to 0.2-0.6 Mpag by a circulating liquid pump at the lower section and then divided into two parts, the first part is sent to a spray pipe at the lower section of the absorption tower, the regenerated flue gas entering the absorption tower is chilled and washed after being atomized by a spray nozzle, and the second part is sent to the regenerated flue gas for spraying and mixing after being fully fluidized by compressed air and then is subjected to the denitration of a second part of catalytic cracking SCR;
in the middle section of the absorption tower, the regenerated flue gas is fully contacted with the middle section circulating liquid added with alkali liquor to remove SO in the flue gas 2 Removing entrainment in wet flue gas by a demister, and then delivering the entrainment to the upper section of an absorption tower; the temperature of the middle circulating liquid discharged from the bottom of the middle section of the absorption tower is 50-65 ℃, the temperature is pressurized to 0.3-0.7 Mpa by a middle circulating liquid pump and then divided into two streams, the first stream is sent to a middle spraying pipe of the absorption tower, the regenerated flue gas entering the absorption tower is washed and absorbed after being atomized by a nozzle, and the second stream is sent to the lower section of the absorption tower to maintain the water balance of the lower section of the absorption tower;
in the upper section of the absorption tower, the wet flue gas is fully contacted with the circulating liquid in the upper section, SO that the residual SO in the flue gas is further removed 2 And salt components in entrainment, and further removing fog drops in the flue gas through a high-efficiency demister, and then discharging the fog drops to the atmosphere; the temperature of the upper circulating liquid discharged from the bottom of the upper section of the absorption tower is 50-65 ℃, the upper circulating liquid is pressurized to 0.4-0.8 Mpag by an upper circulating liquid pump and then is sent to a spray pipe of the upper section of the absorption tower, and the wet flue gas is subjected to secondary washing absorption after being atomized by a nozzle.
2. The catalytic cracking regenerated flue gas sodium alkali desulfurization process according to claim 1, characterized in that: the flow ratio of the first strand of regeneration flue gas to the second strand of regeneration flue gas is 4:1-19:1.
3. The catalytic cracking regenerated flue gas sodium alkali desulfurization process according to claim 1, characterized in that: controlling the flow of the second lower circulation liquid and maintaining the salt content in the lower circulation liquid at 6-16 wt%.
4. The catalytic cracking regenerated flue gas sodium alkali desulfurization process according to claim 1, characterized in that: controlling the flow of the second middle circulating liquid and maintaining the salt content in the middle circulating liquid to be 3-8 wt%.
5. The catalytic cracking regenerated flue gas sodium alkali desulfurization process according to any one of claims 1 to 4, characterized in that: the absorption tower is internally provided with a first baffle and a second baffle which are vertically arranged at intervals, the first baffle and the second baffle divide the absorption tower into an upper section of the absorption tower, a middle section of the absorption tower and a lower section of the absorption tower, the first baffle is provided with a first riser which is vertically arranged and vertically communicated, the upper end of the first riser is positioned above the liquid level of the upper section of the absorption tower, the second baffle is provided with a second riser which is vertically arranged and vertically communicated, and the upper end of the second riser is positioned above the liquid level of the middle section of the absorption tower;
the upper section of the absorption tower is provided with high-efficiency demisters and upper-section spray pipes which are arranged at intervals from top to bottom; the middle section of the absorption tower is provided with foam removers and middle section spray pipes which are arranged at intervals from top to bottom; the lower section of the absorption tower is internally provided with lower section spray pipes and smoke distributors which are arranged at intervals from top to bottom; the inlet of the regeneration flue gas is located at the side wall of the absorber tower and is arranged below the smoke distributor.
6. The catalytic cracking regenerated flue gas sodium alkali desulfurization process according to claim 5, wherein the process is characterized by: the side of absorption tower is provided with the middle section circulating liquid pump, and the entry of this middle section circulating liquid pump is connected with the bottom in absorption tower middle section, and the export of this middle section circulating liquid pump is connected with the middle section shower through first pipeline, is connected and junction is located the liquid level below with the absorption tower hypomere through the second pipeline.
7. The catalytic cracking regenerated flue gas sodium alkali desulfurization process according to claim 5, wherein the process is characterized by: an upper section circulating liquid pump is arranged beside the absorption tower, an inlet of the upper section circulating liquid pump is connected with the bottom of the upper section of the absorption tower, and an outlet of the upper section circulating liquid pump is connected with an upper section spray pipe through a third pipeline.
8. The catalytic cracking regenerated flue gas sodium alkali desulfurization process according to claim 5, wherein the process is characterized by: the absorption tower is characterized by further comprising a buffer tank, a lower section circulating liquid pump is arranged at the side of the absorption tower, an inlet of the lower section circulating liquid pump is connected with the bottom of the lower section of the absorption tower, an outlet of the lower section circulating liquid pump is connected with a lower section spray pipe through a fourth pipeline and connected with the buffer tank through a fifth pipeline, and a top gas phase of the buffer tank is sent to the middle section of the absorption tower.
9. The catalytic cracking regenerated flue gas sodium alkali desulfurization process according to claim 8, characterized in that: the bottom of the buffer tank is fully fluidized by compressed air through a sixth pipeline and a booster pump, and then is sent to be mixed with regenerated flue gas after denitration of the second catalytic cracking SCR.
CN202310036593.6A 2023-01-10 2023-01-10 Sodium alkali desulfurization process for catalytic cracking regenerated flue gas Pending CN116351224A (en)

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