Ammonia desulfurization device for catalytic cracking regenerated flue gas
By combining a supergravity reactor and an absorption tower, the problems of high energy consumption and high ammonia escape in the ammonia desulfurization of catalytic cracking regeneration flue gas are solved, achieving flue gas purification with low energy consumption and low ammonia escape.
Patent Information
- Application Number
- CN202520442734.9
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-03-13
- Publication Date
- 2026-01-30
- Estimated Expiration
- 2035-03-13
AI Technical Summary
Existing catalytic cracking regeneration flue gas ammonia desulfurization technology suffers from high system energy consumption and high ammonia slip.
The system employs a combination of a supergravity reactor and an absorption tower. The supergravity reactor enhances gas-liquid mass transfer and reaction, reduces the amount of absorbent circulating, and the absorption tower performs secondary spray washing to lower the flue gas temperature and reduce ammonia escape.
It significantly reduced the energy consumption and ammonia escape of the equipment, achieving a highly efficient flue gas purification effect.
Smart Images
Figure CN223846637U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model relates to the field of flue gas purification, specifically relates to a catalytic cracking regeneration flue gas ammonia desulfurization device. BACKGROUND
[0002] Carbon will be produced on the surface of catalyst in the process of catalytic cracking and catalytic cracking reaction, and the catalyst needs to enter the regenerator to regenerate to restore activity. Air is usually used to enter the regenerator to burn off the carbon, and the flue gas generated thereby is separated from the entrained catalyst by a cyclone separator, and then discharged after energy recovery by a flue gas turbine and a waste heat boiler. In this process, catalytic cracking regeneration flue gas is produced.
[0003] The existing treatment technology for catalytic cracking regeneration flue gas is mainly sodium alkali desulfurization and ammonia desulfurization technology. When ammonia desulfurization technology is used, the regeneration flue gas needs to be washed by a large amount of absorption liquid circulation to remove particulate matter and sulfides before being discharged into the atmosphere. However, a large amount of absorption liquid circulation will inevitably lead to high system energy consumption and increased operating costs. At the same time, due to the high temperature of the catalytic cracking exhaust gas, the operating temperature of the ammonia desulfurization system is relatively high, which can easily cause ammonia escape and emission problems. SUMMARY
[0004] The utility model aims to overcome the problems of high system energy consumption and high ammonia escape in the existing ammonia desulfurization technology, and provides a catalytic cracking regeneration flue gas ammonia desulfurization device. The device does not need to wash the flue gas with a large amount of absorption liquid circulation, has low energy consumption, and can effectively reduce the problem of ammonia escape.
[0005] To achieve the above-mentioned purpose, the utility model provides a catalytic cracking regeneration flue gas ammonia desulfurization device, which comprises a hypergravity reactor and an absorption tower. The first gas inlet of the hypergravity reactor is connected with the regeneration flue gas. The first liquid inlet of the hypergravity reactor is connected with the absorption liquid. The first gas outlet of the hypergravity reactor is connected with the second gas inlet of the absorption tower. A spray pipe is installed above the second gas inlet in the absorption tower. The tower top of the absorption tower has a second gas outlet.
[0006] In the above technical solution, the regeneration flue gas and the absorption liquid are in contact in the hypergravity reactor. The hypergravity reactor highly strengthens the mass transfer and reaction between the gas and the liquid. The circulation amount of the absorption liquid can be reduced by more than 50%, which greatly reduces the energy consumption and equipment investment of the device. The regeneration flue gas after absorption treatment is further washed and cooled by the liquid sprayed by the spray pipe in the absorption tower, which greatly reduces the problem of ammonia escape and emission.
[0007] Preferably, a demister is installed in the absorption tower. The demister is below the lower section of the absorption tower. The second gas inlet is on the tower wall of the lower section of the absorption tower.
[0008] The absorption tower upper section above the demister is provided with a spray pipe, and a mist eliminator is installed in the absorption tower upper section. With this structure, the regenerated flue gas entering the absorption tower lower section is removed of entrained mist by the demister, and then is sprayed and cooled by the spray pipe, and then is removed of entrained mist by the mist eliminator, and then is discharged through the second gas outlet.
[0009] Preferably, a first liquid outlet at the bottom of the supergravity reactor is connected with the absorption tower lower section, the bottom of the absorption tower lower section is connected with the first liquid inlet of the supergravity reactor through a first pipeline, and a first circulating pump is arranged on the first pipeline. With this structure, the circulating absorption liquid of the supergravity reactor can flow into the absorption tower lower section, which is beneficial to reduce the energy consumption of the device, and the absorption liquid entering the absorption tower lower section is pumped into the supergravity reactor again by the first circulating pump for recycling.
[0010] Preferably, the first pipeline is further connected with a seventh pipeline. With this structure, the circulating absorption liquid is introduced into other treatment units through the seventh pipeline to obtain ammonium sulfate crystals.
[0011] Preferably, the absorption tower lower section is connected with a third pipeline for supplying ammonia and a fourth pipeline for supplying oxidizing air. With this structure, liquid ammonia or ammonia water and oxidizing air are supplemented through the third pipeline and the fourth pipeline.
[0012] Preferably, a liquid receiving plate is installed in the absorption tower upper section between the spray pipe and the demister, the liquid receiving plate is provided with a liquid holding part, a gas lifting cap is arranged on the liquid receiving plate, and the gas lifting cap is provided with a gas lifting hole. With this structure, the regenerated flue gas below the liquid receiving plate rises through the gas lifting hole of the gas lifting cap, and the liquid sprayed by the spray pipe is caught by the liquid receiving plate and does not fall into the absorption tower lower section, which does not interfere with the circulation of the absorption liquid in the absorption tower lower section.
[0013] Preferably, the bottom of the liquid holding part is connected with a second pipeline, the second pipeline is connected with the absorption tower lower section through a fifth pipeline and is connected with the spray pipe through a sixth pipeline, and a second circulating pump is arranged on the second pipeline. With this structure, part of the liquid on the liquid holding part is pumped into the absorption tower lower section by the second circulating pump, and part of the liquid is pumped to the spray pipe for recycling.
[0014] Preferably, a cooler is arranged on the sixth pipeline. With this structure, the liquid pumped to the spray pipe is cooled by the cooler before being sprayed, and the cooled liquid is more conducive to the condensation and precipitation of saturated water, ammonium sulfate and escaped ammonia in the regenerated flue gas, thereby effectively preventing ammonia escape.
[0015] Preferably, the absorption tower upper section is further connected with an eighth pipeline, and an outlet of the eighth pipeline is communicated with the liquid holding part. With this structure, water can be supplemented to the absorption tower upper section through the eighth pipeline when necessary.
[0016] Preferably, the first gas inlet of the supergravity reactor is connected with a dust remover, and the regenerated flue gas is connected with the dust remover.
[0017] By the above technical scheme, the regenerated flue gas is dusted by the dust remover and then contacts with the absorption liquid in the supergravity reactor, so that the mass transfer and reaction process are highly intensified, the circulating absorption liquid amount can be reduced by more than 50%, the energy consumption and equipment investment of the device are greatly reduced, and the regenerated flue gas after washing is further washed and cooled by the liquid sprayed by the spray pipe in the absorption tower, so that the ammonia escape emission problem is greatly reduced. BRIEF DESCRIPTION OF DRAWINGS
[0018] Figure 1 is a structural schematic view of a desulfurization device provided by the utility model;
[0019] Figure 2 is a structural schematic view of a desulfurization device provided by the comparative example.
[0020] BRIEF DESCRIPTION OF DRAWINGS
[0021] 1-dust remover; 2-supergravity reactor; 21-first liquid outlet; 22-first liquid inlet; 23-first gas inlet; 24-first gas outlet; 3-absorption tower; 31-lower section of absorption tower; 32-antifoaming device; 33-upper section of absorption tower; 34-mist eliminator; 35-spray pipe; 36-second gas outlet; 37-second gas inlet; 38-liquid receiving plate; 39-gas lifting cap; 4-first circulating pump; 5-second circulating pump; 6-cooler; 7-first pipeline; 8-seventh pipeline; 9-second pipeline; 10-sixth pipeline; 11-fifth pipeline; 12-third pipeline; 13-fourth pipeline; 14-eighth pipeline. DETAILED DESCRIPTION
[0022] In the description of the present application, it should be understood that the terms "first", "second" and the like are only used for descriptive purposes, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features, so that the features with "first", "second" can be explicitly or implicitly included one or more features. In the description of the present application, unless otherwise stated, the meaning of "multiple" is two or more.
[0023] The terms "upper", "lower", "top", "bottom", "inner", "outer" and the like indicate the orientation or positional relationship shown in the drawings, which is only for the convenience of describing the present application and simplifying the description, and cannot be understood as indicating or implying that the indicated device or element must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as limiting the present application.
[0024] As Figure 1 shown, a catalytic cracking regeneration flue gas ammonia desulfurization device, comprising a supergravity reactor 2 and an absorption tower 3, wherein the first gas inlet 23 of the supergravity reactor 2 is connected with the regeneration flue gas, the first liquid inlet 22 of the supergravity reactor 2 is connected with the absorption liquid, the first gas outlet 24 of the supergravity reactor 2 is connected with the second gas inlet 37 of the absorption tower 3, a spray pipe 35 is installed in the absorption tower 3 and above the second gas inlet 37, and the tower top of the absorption tower 3 has a second gas outlet 36.
[0025] The supergravity reactor comprises a shell, a rotor is arranged in the shell, the rotor is driven by a motor, the side wall of the shell is provided with the first gas inlet 23, a dust collector 1 is connected with the first gas inlet 23, the regeneration flue gas is connected with the dust collector 1, the regeneration flue gas from the dust collector 1 enters the inner cavity of the shell from the tangential direction through the first gas inlet 23, enters the rotor filler from the outer edge of the rotor, the rotor is connected with a liquid phase pipe and a gas phase pipe, wherein the liquid phase pipe is sleeved in the gas phase pipe, the other end of the liquid phase pipe is the first liquid inlet 22, the other end of the gas phase pipe is the first gas outlet 24 and is connected with the second gas inlet 37, the circulating absorption liquid enters the rotor through the first liquid inlet 22 and is sprinkled on the inner edge of the rotor, the absorption liquid is dispersed by the filler, thereby improving the mass transfer and reaction process with the regeneration flue gas, and the shell bottom has the first liquid outlet 21, the circulating absorption liquid is discharged from the first liquid outlet 21.
[0026] A defoamer 32 is installed in the absorption tower 3, the absorption tower lower section 31 is below the defoamer 32, the tower wall of the absorption tower lower section 31 has the second gas inlet 37, the absorption tower upper section 33 is above the defoamer 32, the spray pipe 35 is located in the absorption tower upper section 33, and a demister 34 is also installed in the absorption tower upper section 33 and is located above the spray pipe 35.
[0027] The first liquid outlet 21 of the bottom of the supergravity reactor 2 is connected with the absorption tower lower section 31, the bottom of the absorption tower lower section 31 is connected with the first liquid inlet 22 of the supergravity reactor 2 through a first pipeline 7, a first circulating pump 4 is arranged on the first pipeline 7, and the first pipeline 7 is also connected with a seventh pipeline 8.
[0028] The absorption tower lower section 31 is connected with a third pipeline 12 for ammonia and a fourth pipeline 13 for oxidizing air.
[0029] A liquid receiving plate 38 is arranged in the upper section 33 of the absorption tower between the spray pipe 35 and the demister 32, and a liquid holding part is formed on the liquid receiving plate 38 for receiving the circulating absorption liquid, and a gas lifting cap 39 is arranged on the liquid receiving plate 38, and the gas lifting cap 39 has gas lifting holes.
[0030] In order to facilitate water supplement, the upper section 33 of the absorption tower is further connected with an eighth pipeline 14, and the outlet of the eighth pipeline 14 is communicated with the liquid holding part.
[0031] The working process of the device is as follows: the regenerated flue gas with a temperature of 150-250 DEG C, a pressure of 0.004-0.01 MPaG, SO2 content of 500-3000 mg / Nm 3 , and particulate matter content of 100-1000 mg / Nm 3 enters the dust remover 1, and the particulate matter content in the flue gas can be reduced to 1-20 mg / Nm 3 , then enters the supergravity reactor 2, and the liquid-gas ratio of the circulating absorption liquid flow and the regenerated flue gas flow in the supergravity reactor 2 is 2-5 L / Nm 3 , and the supergravity environment with a centrifugal force of 10-1000 g can be formed in the supergravity reactor 2, so that the SO2 in the regenerated flue gas is effectively removed, the regenerated flue gas out of the supergravity reactor 2 is sent into the absorption tower 3, enters the upper section 33 of the absorption tower through the gas lifting cap after removing the mist by the demister 32, and the temperature of the regenerated flue gas is reduced to 45-60 DEG C after being washed by the liquid sprayed by the spray pipe 35, the SO2 content in the flue gas is ≤20 mg / Nm 3 , the particulate matter content is ≤10 mg / Nm 3 , and the ammonia escape is ≤2 mg / Nm 3 , and the regenerated flue gas can be discharged up to the standard.
[0032] The circulating absorption liquid in the supergravity reactor 2 is contacted with the regenerated flue gas, and the temperature is reduced to 50-65 DEG C, and the circulating absorption liquid flows into the lower section 31 of the absorption tower by itself, the circulating absorption liquid in the lower section 31 of the absorption tower is pressurized to 0.2-0.8 MPaG by the first circulating pump 4, and part of the circulating absorption liquid is sent into the supergravity reactor for circulation, and the other part is sent to the ammonium sulfate crystallization unit, and the ammonium sulfate content in the circulating absorption liquid is maintained at 8-25 wt%.
[0033] The liquid in the upper section of the absorption tower is pressurized to 0.4-0.8 MPaG by the second circulating pump 5, and part of the liquid is sent to the lower section of the absorption tower for circulation, and the other part is cooled to 40-50 DEG C by the cooler 6 and then sent to the spray pipe 35 for circulation.
[0034] The regenerated flue gas with temperature 170℃, pressure 0.004MPaG, SO2 content 780mg / Nm 3 , particulate content 230mg / Nm 3 is taken as an example, and the particulate content is lowered to 5mg / Nm 3 after dust removal by the dust remover 1 3 , the liquid-gas ratio in the supergravity reactor 2 is controlled to be 3L / Nm 3 , the absorption liquid pressure is 0.4MPaG after pressurization by the first circulating pump 4, and the liquid pressure is 0.7MPaG after pressurization by the second circulating pump 5, air and ammonia water are supplemented to the lower section of the absorption tower, water with temperature 25℃ and pressure 0.7MPaG is supplemented to the upper section of the absorption tower, the ammonium sulfate content in the absorption liquid circulating in the lower section of the absorption tower is controlled to be 8wt%, and the SO2 content in the purified flue gas finally discharged is 15mg / Nm 3 , the particulate content is 5mg / Nm 3 , and the ammonia escape is 1mg / Nm
[0035] When the device is used to treat the regenerated flue gas in the example, the total absorption liquid circulating in the absorption tower is 1350m 3 / h, the liquid-gas ratio of the total absorption liquid in the absorption tower and the regenerated flue gas is 3, the power of the first circulating pump 4 is 113kW, the flue gas temperature finally discharged is 50℃, and the ammonia escape is only 1mg / Nm 3 .
[0036] The structure shown in Figure 2 is taken as a comparison, and the difference from Figure 1 is that the regenerated flue gas does not pass through the supergravity reactor, but directly enters the absorption tower 3 after the dust remover 1, and at least 2-3 levels of spray structures are arranged in the lower section of the absorption tower 3 from bottom to top in sequence for spraying, it is found that the total absorption liquid consumption in the absorption tower is as high as 3150m 3 / h, the liquid-gas ratio of the absorption liquid and the regenerated flue gas is as high as 7, the power of the first circulating pump 4 is as high as 380kW, the flue gas temperature finally discharged is 55℃, and the ammonia escape is as high as 3mg / Nm 3 . It can be seen that the energy consumption and ammonia escape rate of the device provided by the utility model are significantly reduced.
[0037] The preferred embodiments of the utility model are described in detail above in combination with the drawings, but the utility model is not limited thereto. Within the technical concept range of the utility model, the technical scheme of the utility model can be subjected to various simple modifications, for example, the lifting structure can be changed into other mechanical lifting structures, various specific technical features are combined in any suitable manner, in order to avoid unnecessary repetition, the utility model will not be described again for various possible combination manners. However, the simple modifications and combinations should also be regarded as the disclosed contents of the utility model, and all belong to the protection range of the utility model.
Claims
1. A catalytic cracking regeneration flue gas ammonia process desulfurization device, characterized in that, The application relates to a high-gravity reactor and an absorption tower, wherein the first gas inlet of the high-gravity reactor is connected with regenerated flue gas, the first liquid inlet of the high-gravity reactor is connected with absorption liquid, the first gas outlet of the high-gravity reactor is connected with the second gas inlet of the absorption tower, a spray pipe is arranged in the absorption tower and above the second gas inlet, and the top of the absorption tower is provided with a second gas outlet.
2. The apparatus of claim 1, wherein, A demister is arranged in the absorption tower, and the demister is below the lower section of the absorption tower, and the tower wall of the lower section of the absorption tower is provided with the second gas inlet. The upper section of the absorption tower is above the demister, the spray pipe is arranged in the upper section of the absorption tower, and a mist eliminator is arranged in the upper section of the absorption tower.
3. The apparatus of claim 2, wherein, The first liquid outlet at the bottom of the high-gravity reactor is connected with the lower section of the absorption tower, the bottom of the lower section of the absorption tower is connected with the first liquid inlet of the high-gravity reactor through a first pipeline, and a first circulating pump is arranged on the first pipeline.
4. The apparatus of claim 3, wherein, The first pipeline is further connected with a seventh pipeline.
5. The apparatus of any of claims 2-4, wherein, The lower section of the absorption tower is connected with a third pipeline for ammonia and a fourth pipeline for oxidizing air.
6. The apparatus of claim 5, wherein, A liquid receiving plate is arranged in the upper section of the absorption tower between the spray pipe and the demister, the liquid receiving plate is provided with a liquid holding part, the liquid receiving plate is provided with a gas lifting cap, and the gas lifting cap is provided with gas lifting holes.
7. The apparatus of claim 6, wherein, The bottom of the liquid holding part is connected with a second pipeline, the second pipeline is connected with the lower section of the absorption tower through a fifth pipeline and connected with the spray pipe through a sixth pipeline, and a second circulating pump is arranged on the second pipeline.
8. The apparatus of claim 7, wherein, A cooler is arranged on the sixth pipeline.
9. The apparatus of claim 6, wherein, The upper section of the absorption tower is further connected with an eighth pipeline, and the outlet of the eighth pipeline is communicated with the liquid holding part.
10. The apparatus of any of claims 1-4 and 6-9, wherein, A dust remover is arranged on the first gas inlet of the high-gravity reactor, and the regenerated flue gas is connected with the dust remover.