CN118059666A - Novel catalytic cracking flue gas integrated dust removal desulfurizing tower - Google Patents
Novel catalytic cracking flue gas integrated dust removal desulfurizing tower Download PDFInfo
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- CN118059666A CN118059666A CN202410253460.9A CN202410253460A CN118059666A CN 118059666 A CN118059666 A CN 118059666A CN 202410253460 A CN202410253460 A CN 202410253460A CN 118059666 A CN118059666 A CN 118059666A
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- 239000000428 dust Substances 0.000 title claims abstract description 110
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 102
- 239000003546 flue gas Substances 0.000 title claims abstract description 102
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 21
- 230000003009 desulfurizing effect Effects 0.000 title claims description 19
- 239000007921 spray Substances 0.000 claims abstract description 169
- 239000007788 liquid Substances 0.000 claims abstract description 111
- 238000010521 absorption reaction Methods 0.000 claims abstract description 90
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- 238000010791 quenching Methods 0.000 claims abstract description 75
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- 238000011010 flushing procedure Methods 0.000 claims abstract description 33
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- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical class S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
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Abstract
The invention provides a catalytic cracking flue gas integrated dust removal desulfurization tower which comprises a tower body, a chimney, a reducing section, a high-efficiency dust removal demister, a three-stage spray multi-pipe type array Guan Chuchen, a two-stage spray absorption section, a first-stage spray quenching section and a tower bottom slurry oxidation section which are sequentially arranged from top to bottom, wherein the first-stage spray quenching section is provided with a flue gas inlet, and the top of the chimney is provided with a flue gas outlet. The primary spraying quenching section is provided with a plurality of quenching spray heads, the secondary spraying absorption section is provided with a plurality of layers of absorption section spray heads, and slurry is sprayed to cool flue gas in a quenching way, remove dust and desulfurize; the three-stage spraying multi-pipe type column Guan Chuchen device is provided with a plurality of venturi pipes and three-stage spraying pipes, fine particles are coagulated, and dust removal is intercepted under the action of spraying slurry; the high-efficiency dust and mist remover is provided with a plurality of cyclone tube bundles and water spray flushing pipes, so that the flue gas is centrifugally separated, tiny particles are condensed and collide, and the tiny particles are captured by a liquid film to absorb dust and mist remover. The device has compact structure and high efficiency, and can meet the operation requirement of high-efficiency dust removal and desulfurization.
Description
Technical Field
The invention belongs to the technical field of catalytic cracking flue gas treatment, and particularly relates to a novel catalytic cracking flue gas integrated dust removal desulfurization tower.
Background
Catalytic Cracker (FCCU) feedstock typically contains sulfur-containing compounds such as mercaptans, sulfides, cyclic sulfides, thiophenols, thiophenes, and the like. In the catalytic cracking reaction process, part of the sulfur-containing compounds are converted into hydrogen sulfide (H 2 S), thiophene and the like which exist in reaction oil gas and oil products, and part of the sulfur-containing compounds are converted into condensate which has a complex structure and relatively large molecular mass and exist in slurry oil and coke. Sulfur in the coke is combusted to form sulfur oxides (SO X) whose concentration is related to the sulfur content of the feedstock, the source of the feedstock, the coke yield, and the mode of regeneration, among other things. The flue gas generated by the oxidation reaction of the sulfur-containing coke in the regenerator will pollute the atmosphere if directly discharged. And the catalytic cracking regenerated flue gas has the characteristics of high flue gas temperature, large fluctuation of dust content and enrichment of finer and hard catalytic cracking catalyst particles, and is one of main pollutant emission sources of oil refineries.
Catalytic cracking regeneration flue gas generally has the following characteristics: (1) The fluctuation of the NOx and SO X content is large, the SO X concentration is generally 700-4500 mg/Nm 3, and the NOx concentration is generally 50-400 mg/Nm 3. (2) The temperature of the regenerated flue gas is relatively high, the normal temperature is 180-230 ℃, and the highest temperature can reach 350-500 ℃ when the catalytic waste heat boiler or the CO boiler fails; (3) the concentration fluctuation of the particulate matters in the flue gas is large. Under normal working conditions, the concentration of the particles is generally 150-300 mg/Nm 3 after passing through the three-stage cyclone separator and the four-stage cyclone separator; when the waste heat boiler or the CO boiler is blown to ash regularly, the maximum concentration can reach 3000-4000 mg/Nm 3; (4) Most of the particles in the flue gas are catalysts, the particle size distribution is small, the particle size of 0-5 mu m accounts for more than 70%, and the hardness is high. (5) The flue gas dust removal desulfurization device is usually arranged at the tail end of the FCCU flow and operates synchronously with the FCCU, and the pressure drop of the dust removal desulfurization device can influence the upstream operation and directly influence the operation cost and economic benefit of the FCCU. (6) Most of the prior FCCU designs do not reserve the position of flue gas dust removal and desulfurization facilities, and meanwhile, the distance between a catalytic waste heat boiler or a CO boiler and a chimney is short, and the plane and the space are limited. Because of the characteristics of the catalytic cracking regenerated flue gas, the catalytic cracking regenerated flue gas has more severe technical requirements on dust removal and desulfurization.
Because of the characteristics of catalytic cracking flue gas, wet dust removal becomes a main choice for removing catalyst dust from catalytic flue gas in order to meet the increasingly strict emission standard, and because wet desulfurization has higher desulfurization efficiency, the wet scrubbing integrated technology is currently the main stream of catalytic cracking flue gas dust removal and desulfurization.
However, in the existing wet dust removal and desulfurization integrated equipment, there is still some shortages and improvement room, such as SO X and particulate matters in catalytic cracking flue gas, and the removal efficiency of the equipment needs to be further improved, especially for the conditions of large fluctuation of inlet flue gas working conditions and fine particles in the particulate matters. Meanwhile, the removal of a large amount of fog drops contained in the flue gas after desulfurization and dust removal is still to be further improved and improved. Therefore, the development of the integrated equipment for wet dedusting and desulfurization of the catalytic cracking flue gas, which meets the current industry requirements, has very important significance.
Disclosure of Invention
The invention aims to overcome the defects in the prior art, and provides a novel catalytic cracking flue gas integrated dust removal desulfurization tower which integrates dust removal and desulfurization of flue gas, has a compact structure, and can meet the operation requirements of efficient dust removal and desulfurization and efficiently remove SO X and particles with different particle diameters in the flue gas.
The technical scheme provided by the invention is as follows:
The utility model provides a catalytic cracking flue gas integration dust removal desulfurizing tower, integration dust removal desulfurizing tower includes the tower body, set gradually top of the tower chimney, reducing section, high-efficient dust removal defogging drip ware, tertiary spraying multitube row Guan Chuchen ware, second grade spray absorption section, one-level spray quench section and tower bottom thick liquid oxidation section from top to bottom on the tower body, the top of the tower chimney sets up and purifies the flue gas export, one-level spray quench section sets up the flue gas import, wherein:
A plurality of quenching spray nozzles are arranged on the tower wall of the primary spraying quenching section or the flue gas inlet, the inlets of the quenching spray nozzles are connected with a quenching spray pipe and are used for supplying and conveying circulating absorption slurry from the tower bottom to the quenching spray nozzles, and the whole cross section of the flue gas inlet is fully covered by spraying the slurry through the quenching spray nozzles, SO that the flue gas is cooled rapidly and SO X is removed;
The secondary spraying absorption section comprises a plurality of layers of absorption section spraying from bottom to top, each layer of absorption section spraying is provided with a plurality of absorption section spray nozzles, an absorption section spray pipe connected with an inlet of the absorption section spray nozzle is connected with the tower wall of the secondary spraying absorption section and is used for supplying and conveying circulating absorption slurry from the tower bottom to the absorption section spray nozzles, and the whole cross section in the tower is fully covered by spraying the slurry through the absorption section spray nozzles, SO that flue gas is washed and dedusted and SO X is removed;
The three-stage spray multi-tube type tube nest dust remover comprises a dust remover liquid collecting tank, a plurality of parallel venturi tubes and a three-stage spray tube, wherein the periphery of the bottom plate of the dust remover liquid collecting tank is connected with the inner wall of the tower body, the venturi tubes penetrate through the bottom plate of the dust remover liquid collecting tank to be fixedly arranged, and the three-stage spray tube is arranged above the venturi tubes and is used for removing fine particles carried in rising flue gas by utilizing a venturi structure, gathering the fine particles into large particles, intercepting and washing the large particle dust under the spray action, and removing SO 3 carried in liquid drops;
The efficient dedusting and mist-removing device comprises a plurality of cyclone cylinder tube bundles which are arranged in parallel and a plurality of water spraying flushing pipes which are arranged above the cyclone cylinder tube bundles, wherein the cyclone cylinder tube bundles comprise a plurality of cyclone cylinders which are overlapped in series along the vertical direction, cyclone plates are arranged in the cyclone cylinders and are used for rotating and centrifugally separating ascending flue gas in the cyclone cylinders, and tiny particles are condensed into large liquid drops which collide with the cyclone cylinder walls of which the surfaces are sprayed and wetted by water, and are captured and absorbed by liquid films to realize dedusting and mist-removing;
the tower bottom slurry oxidation section comprises a tower bottom liquid collecting tank and an oxidation wind distributor, wherein the periphery of the bottom plate of the tower bottom liquid collecting tank is connected with the inner wall of the tower body, and the oxidation wind distributor is arranged above the tower bottom liquid collecting tank and is respectively used for storing tower bottom slurry and oxidizing the tower bottom slurry.
The invention is further arranged that the operation temperature of the integrated dedusting and desulfurizing tower is 50-65 ℃ and the operation pressure is about 3500-5000 Pa (G). The tower body is made of an acid-resistant and wear-resistant metal material (such as 304L), a carbon steel lining acid-resistant and wear-resistant metal material (such as 304L) or a carbon steel lining nonmetal material (such as a carbon steel lining PTU), and the smoke inlet is made of a high-temperature-resistant and acid-resistant alloy material.
The invention is further arranged that the flue gas inlet is connected with the tower wall of the primary spraying quenching section, the connection included angle between the flue gas inlet and the tower wall is 30-90 degrees, preferably 60-90 degrees, more preferably 90 degrees, namely the flue gas inlet is vertically connected with the tower wall of the primary spraying quenching section.
The invention is further arranged that the quenching spray head is arranged on the tower wall of the primary spraying quenching section and is connected with the tower wall at a certain angle; wherein, part of quenching spray heads are arranged on the upper side and the lower side of the flue gas inlet and are vertical to the direction of the flue gas inlet at an angle of 90 degrees, and part of quenching spray heads are arranged on the left side and the right side of the flue gas inlet and are arranged at an angle of 15 degrees to 90 degrees, preferably 15 degrees to 30 degrees, with the direction of the flue gas inlet.
The invention is further characterized in that the two-stage spray absorption section is provided with 1-5 layers of absorption section spray, and each layer of absorption section spray is provided with 3-5 absorption section spray heads. The absorption section spray nozzles of each layer are uniformly arranged on the same plane, and the included angle between the absorption section spray pipe and the horizontal direction is 1-10 degrees, preferably 3-6 degrees, and preferably is downward along the horizontal direction. The spraying of each two adjacent layers of absorption sections is in staggered arrangement at a certain angle, and the included angle of the spraying of each two layers of absorption sections is 10-50 degrees, preferably 15-30 degrees.
The invention is further arranged that the bottom plate of the dust collector liquid collecting tank is welded on the inner wall of the tower body at an inclined angle of 10-30 degrees with the horizontal direction; the bottom of the slope of the liquid collecting tank of the dust collector is provided with a liquid storage area with a certain volume, the liquid storage height of the liquid storage area is 0.5-1.2 m, and the liquid storage area is provided with a liquid collecting tank outlet of the dust collector towards the outer side of the wall surface of the tower body.
The invention is further arranged that the lower part of the venturi tube is fixed on the bottom plate of the dust collector liquid collecting tank through welding or flange connection; the venturi tubes are fixedly connected through rib plates. The lower end of each venturi tube is connected with a guide vane segment, and guide vanes are arranged in the venturi tube, so that ascending smoke gas is enabled to rise in the venturi tube in a rotating mode. And a dust collector overflow pipe is fixedly arranged on the bottom plate penetrating through the dust collector liquid collecting groove, the bottom end of the dust collector overflow pipe penetrates through the wall surface of the tower body, and an overflow liquid outlet is arranged.
The invention is further provided with 1-50 tertiary spray pipes, preferably 0.5-1.5 m at the upper end of the venturi pipe. The three-stage spray pipes are downwards connected with a plurality of spray nozzles, and each spray nozzle corresponds to one venturi pipe. The inlet of the third-stage spray pipe is provided with a plurality of third-stage spray pipe liquid inlets which are positioned on the wall surface of the tower body and connected with the outlet of the liquid collecting tank of the dust remover through a circulating pump, and the slurry collected by the liquid collecting tank of the dust remover is circularly sprayed in the third-stage spray multi-pipe type tube nest dust remover.
The invention further provides that in the efficient dedusting and demisting drip catcher, each water spray flushing pipe is connected with a plurality of water spray hoses, a plurality of flushing nozzles are arranged in each cyclone cylinder, and each flushing nozzle is respectively connected with the water spray flushing pipe through the water spray hose, so that the wall of each cyclone cylinder is wetted by spray flushing water.
The invention is further characterized in that 2-3 cyclone cylinders are arranged in each cyclone cylinder tube bundle, and 2-4 flushing nozzles are arranged in each cyclone cylinder. And the water spraying flushing pipe is arranged at a position 0.5-1.2 m above the cyclone cylinder tube bundle.
The invention is further arranged that the bottom plate of the tower bottom liquid collecting tank is welded on the inner wall of the tower body at an inclined angle of 15-60 degrees with the horizontal direction, and preferably 15-30 degrees. The bottom of the slope of the tower bottom liquid collecting tank is provided with a tower bottom slurry outlet towards the outer side of the wall surface of the tower body, and the tower bottom slurry outlet is connected with the quenching spray head and the absorption section spray head through a circulating pump to provide circulating slurry for spraying in the primary spraying quenching section and the secondary spraying absorption section.
The invention is further characterized in that the inlet of the oxidation wind distributor is provided with a plurality of oxidation wind inlets which are positioned on the wall surface of the tower body and connected with an external oxidation fan. The oxidation wind distributor comprises a plurality of oxidation wind main pipes and a plurality of oxidation wind branch pipes, wherein a plurality of wind outlet holes are formed in the oxidation wind branch pipes at equal intervals, the diameter of each wind outlet hole is 50-150 mm, and the distance between every two adjacent wind outlet holes is 0.5-800 mm. The relative distance between the oxidation wind distributor and the tower bottom plate is determined according to the liquid level height of the liquid stored in the tower bottom slurry oxidation section, and the distance between the oxidation wind distributor and the tower bottom plate is generally 0.5-2.0 m; the distance from the level of the stored liquid is 5 to 10m, preferably 6 to 8m.
The invention is further characterized in that a tower bottom oxidizing liquid return pipe is arranged above the bottom plate of the tower bottom liquid collecting tank and near the bottom plate, the oxidizing liquid return pipe is arc-shaped and is arranged along the wall surface of the tower body, and a plurality of liquid outlet holes are formed in the tower bottom oxidizing liquid return pipe at equal intervals and are used for flushing the bottom plate of the tower bottom liquid collecting tank by slurry return; the diameter of the liquid outlet hole is 50-200 mm, and the distance between the adjacent liquid outlet holes is 0.56-1.2 m.
The invention is further characterized in that a plurality of temperature detection instrument interfaces are arranged on the tower wall of the primary spraying quenching section and are arranged at the position of the tower wall opposite to the flue gas inlet. The connection included angle between the temperature detection instrument interface and the tower wall is 90 degrees, the temperature detection instrument interface is arranged up and down, and the interval between the interfaces is 0.5-2.0 m.
The invention is further provided that the upper tower wall of the secondary spraying absorption section, the tower wall of the upper part of the three-stage spraying multi-pipe type tube nest dust remover and the tower wall of the upper part of the high-efficiency dust and mist remover are respectively provided with a pressure detection instrument interface, and the lower tower wall of the tower top chimney is provided with a CEMS detection instrument interface; the included angle between the joint of the instrument interface and the tower wall is 15-60 degrees, preferably 30-45 degrees, and is preferably arranged upwards along the horizontal direction in order to avoid the interface blockage.
Compared with the prior art, the invention has the beneficial effects that:
(1) The invention has the advantages of integrated dust removal and desulfurization, short process flow in the tower, small resistance reduction and high efficiency. And hierarchical treatment is adopted, SO that SO X and particulate matters and dust with different particle diameters in the flue gas are treated in a hierarchical manner by arranging a primary spraying quenching section, a secondary spraying absorption section, a tertiary spraying multi-pipe type tube array dust remover and a high-efficiency dust removing and mist removing device, and the desulfurization efficiency and the long period stability of the particulate matters and dust reach the standard are ensured.
(2) The integrated dedusting and desulfurizing tower adopts special structural design, and comprises a main tower inner quenching spray head, an absorption section spray head, a multi-tube type shell and tube dust remover and a spray head thereof, a high-efficiency dedusting and demisting device and a flushing nozzle thereof and other structural settings, wherein the integrated dedusting and desulfurizing tower realizes the effects of quenching and cooling flue gas and high-efficiency desulfurizing and dedusting at the same time. The quenching spray head and the absorption section spray head are large-caliber non-atomizing spray heads, and the multi-layer flat cone-shaped torrent water curtain formed by the large-caliber spray heads can reduce the temperature of flue gas to saturation and wash large-particle high-concentration particles at the same time, so that the dust removal and desulfurization effects can be ensured even under the condition of running agent operation of the catalytic cracking device.
(3) The primary spraying quenching section adopts the quenching spray heads with special structural design, and a plurality of quenching spray heads are arranged at the smoke inlet at a special angle, SO that the flat cone-shaped torrent water curtain sprayed by each spray head is overlapped at multiple angles, the cross section of the smoke inlet is fully covered, and the high-temperature smoke passes through the torrent water curtain and simultaneously achieves the effects of quenching, cooling, absorbing SO 2 and removing large particles.
Because the quenching spray nozzle is arranged on the tower wall or the flue gas inlet, the formation of the torrent water curtain can continuously wash the tower wall, the flue gas and the slurry are contacted with the acidic and particle-containing liquid formed on the tower wall to wash and fall into the tower bottom liquid collecting tank, the corrosion and abrasion of a dry-wet interface of the inlet section of the integrated dedusting and desulfurizing tower are effectively avoided, the high-temperature damage of high-temperature flue gas to the inlet section of the washing tower is effectively prevented, and the service life and the stability of the washing tower are greatly improved.
(4) The secondary spraying absorption section adopts a special structural design, the absorption section is provided with 1-5 layers of absorption section spraying according to the requirements of the treated flue gas amount from bottom to top, spray heads and spray pipes of the absorption section are connected with the tower wall at a certain angle, a plurality of annular spray heads of each layer spray slurry to form a torrent water curtain in a flat cone curtain shape to fully cover the inner cross section of the tower, the layers and the interlayer spray heads are arranged in a staggered manner at a certain angle, the barrel of the secondary spraying absorption section is fully covered, and the special structural design ensures that flue gas is rapidly and intensively collided and closely contacted with liquid drops in the torrent water curtain, so that coarse particles are effectively removed, and chemical reaction desulfurization is rapidly carried out.
And the spray forming the torrent water curtain can continuously wash the tower wall, so that the flue gas and the slurry are contacted with the acidic and particle-containing liquid formed on the tower wall to wash and fall into the slurry pool at the bottom of the tower, thereby effectively preventing the corrosion and abrasion of the integrated dust removal desulfurization tower wall.
(5) The three-stage multitube type tube nest dust remover adopts a special structural design, a liquid collecting groove in the three-stage multitube type tube nest dust remover is welded on a main tower at a certain angle, a plurality of venturi tubes are arranged on a groove plate, a guide vane is arranged at the inlet of each venturi tube to enable smoke to rise in a rotating way, the smoke is subjected to primary centrifugal separation, and fine particles and water drops are removed; the venturi principle is utilized, the relative flow velocity between the two phases of gas and liquid in the shrinkage tube and the venturi tube is large, the gas is saturated by water, and the gas film attached to the surface of dust particles is broken through, so that the dust particles are wetted by the water, and therefore, violent collision and agglomeration occur between the dust particles and liquid drops or dust particles; in the diffuser pipe, the reduction of the air flow speed and the return of the pressure make the agglomeration of dust particles as condensation nuclei occur faster and become larger-particle-size dust-containing liquid drops.
The upper part of the venturi tube is provided with spray nozzles which are not atomized at a certain height, each spray nozzle corresponds to one venturi tube, the venturi tube is gathered into large-particle fine dust by utilizing a high-density conical water film sprayed by the spray nozzles to intercept and wash, the effect of efficiently removing the fine dust is achieved, and meanwhile, SO 3 carried in liquid drops and trace heavy metals carried by flue gas can be removed. The high-density conical water film sprayed by the spray nozzle has the advantages of stable form, strong shock resistance, difficult scattering of the water curtain and the like.
(6) The invention adopts the high-efficiency dust-removing and mist-removing device to eliminate the phenomenon of rain in a chimney; the structure comprises a plurality of cyclone tube bundles, a plurality of stages of cyclone tubes are arranged in each cyclone tube bundle, cyclone plates are arranged in the cyclone tubes to enable desulfurized clean flue gas to rotate in the cyclone tubes, and the principle of centrifugal separation is utilized to form violent rotation and disturbance of gas-liquid two phases above the cyclone, so that tiny liquid drops, tiny dust particles, aerosol and other tiny particles in the clean flue gas collide mutually and agglomerate to form large liquid drops, and then under the action of the cyclone plate external rotating structure, the dedusting desulfurized clean flue gas is enabled to move outwards in a centrifugal mode, the large liquid drops formed by polymerization collide with the cyclone tube wall and are captured and absorbed by a liquid film formed by flushing water on the cyclone tube wall, and high-efficiency demisting and dedusting are realized.
(7) The tower bottom slurry oxidation section is provided with an oxidation wind distributor, and the circulating absorption slurry is subjected to primary oxidation in the tower so as to meet the standard of COD (chemical oxygen demand) emission of discharged wastewater.
Drawings
FIG. 1 is a schematic structural view of a catalytic cracking flue gas integrated dust removal desulfurization tower of the invention;
FIG. 2A is a schematic view (top view) of a portion of the nozzle arrangement in the primary spray quench section of the present invention;
FIG. 2B is a schematic view (top view) of a portion of the nozzle arrangement in the primary spray quench section of the present invention;
FIG. 2C is a schematic elevation view of a primary spray quench section of the present invention;
FIG. 3A is a schematic elevation view of an absorption section spray in a secondary spray absorption section of the present invention;
FIG. 3B is a top view of the absorber spray in the secondary spray absorber of the present invention;
FIG. 4A is a schematic elevational view of a three stage spray multitube tubulation dust collector of the present invention;
FIG. 4B is a top view of the venturi in the three stage spray multitube in-tube dust collector of the present invention;
FIG. 4C is a top view of a tertiary spray pipe in a tertiary spray multi-pipe column dust collector of the present invention;
FIG. 5A is a top view of a water spray rinse tube in the high efficiency dust and mist eliminator of the present invention;
FIG. 5B is a schematic elevational view of the high efficiency dust and mist eliminator of the present invention;
FIG. 5C is a top view of a cyclone tube bundle in a high efficiency dedusting and mist eliminator according to the present invention;
FIG. 6A is a top view of an oxidation wind distributor in the bottom slurry oxidation section of the present invention;
Fig. 6B is a top view of the bottom oxidizing liquid return conduit in the bottom slurry oxidation stage of the present invention.
Wherein, 1, the tower body; 2. a tower top chimney; 3. a reducing section; 4. a high-efficiency dust and mist remover; 5. three-stage spray multitube array Guan Chuchen; 6. a second-stage spray absorption section; 7. a primary spraying quenching section; 8. a tower bottom slurry oxidation section; 11-16, an inspection manhole; 21. a purified flue gas outlet; 22. CEMS detection instrument interface; 41. a cyclone tube bundle; 42. a water spray flushing pipe; 43. a spray rinse water inlet; 45. a water spray hose; 46. flushing the nozzle; 47. a third pressure sensing instrument interface; 51. a dust collector liquid collecting tank; 52. a venturi tube; 53. a guide vane segment; 54. an overflow pipe of the dust remover; 55. an overflow liquid outlet; 56. an outlet of a liquid collecting tank of the dust remover; 57. a third-stage spray pipe; 58. a liquid inlet of the three-stage spray pipe; 59. spraying nozzle; 60. a second pressure sensing instrument interface; 61-65, absorbing section spraying (absorbing section spray head and absorbing section spray pipe); 67. a first pressure sensing instrument interface; 71. a flue gas inlet; 72. quenching spray head; 73. a temperature detection instrument interface; 74. quenching spray pipe; 81. a bottom sump; 82. a bottom slurry outlet; 83. an oxidation wind distributor; 84. an oxidation wind inlet; 85. a tower returning slurry inlet; 86. a bottom oxidation liquid return pipe; 87. an air outlet hole; 88. an overflow port; 89. and a liquid outlet hole.
Detailed Description
The technical scheme of the invention is clearly and completely described in the following by specific embodiments. It is to be understood that the described embodiments are only some, but not all, of the embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to fall within the scope of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art.
Example 1
The invention provides a catalytic cracking flue gas integrated dust removal desulfurization tower, as shown in fig. 1, the integrated dust removal desulfurization tower comprises a tower body 1, a tower top chimney 2, a reducing section 3, a high-efficiency dust removal demister 4, a three-stage spray multi-pipe type tubular dust remover 5, a two-stage spray absorption section 6, a first-stage spray quenching section 7 and a tower bottom slurry oxidation section 8 are sequentially arranged on the tower body 1 from top to bottom, a purified flue gas outlet 21 is arranged at the top of the tower top chimney 2, and a flue gas inlet 71 is arranged at the first-stage spray quenching section 7, wherein:
A plurality of quenching spray nozzles 72 are arranged on the tower wall of the primary spraying quenching section 7 or on the cylinder body of the flue gas inlet 71, and as shown in the combination of fig. 2A-2C, the inlets of the quenching spray nozzles 72 are connected with a quenching spray pipe 74 for supplying and conveying circulating absorption slurry from the tower bottom to the quenching spray nozzles 72, and the whole cross section of the flue gas inlet 71 is fully covered by spraying the slurry through the quenching spray nozzles 72, SO that the flue gas is cooled rapidly and SO X is removed;
The secondary spraying absorption section 6 comprises a plurality of layers of absorption section spraying from bottom to top, each layer of absorption section spraying is provided with a plurality of absorption section spray nozzles, an absorption section spray pipe connected with an inlet of the absorption section spray nozzle is connected with the tower wall of the secondary spraying absorption section 6 and is used for supplying and conveying circulating absorption slurry from the tower bottom to the absorption section spray nozzles, and the whole cross section in the tower is fully covered by spraying the slurry through the absorption section spray nozzles, SO that flue gas is washed and dedusted and SO X is removed;
The three-stage spraying multi-tube type column dust remover 5 comprises a dust remover liquid collecting tank 51, a plurality of venturi tubes 52 and a three-stage spraying tube 57, wherein the periphery of the bottom plate of the dust remover liquid collecting tank 51 is connected with the inner wall of the tower body 1, the venturi tubes 52 penetrate through the bottom plate of the dust remover liquid collecting tank 51 and are fixedly arranged in parallel, the three-stage spraying tube 57 is arranged above the venturi tubes 52 and is used for removing fine particles carried in rising flue gas by utilizing a venturi structure, gathering the fine particles into large particles, intercepting and washing the large particle dust under the spraying action, and meanwhile removing SO 3 carried in liquid drops;
The efficient dedusting and mist-removing device 4 comprises a plurality of cyclone cylinder tube bundles 41 which are arranged in parallel and a plurality of water spraying flushing pipes 42 which are arranged above the cyclone cylinder tube bundles 41, wherein the cyclone cylinder tube bundles 41 comprise a plurality of cyclone cylinders which are overlapped in series along the vertical direction, cyclone plates (not shown in the figure) are arranged in the cyclone cylinders and are used for rotating and centrifugally separating rising flue gas in the cyclone cylinders, and tiny particles are condensed into large liquid drops to collide with the cyclone cylinder walls of which the surfaces are sprayed and wetted by water, so that dedusting and mist-removing are realized by being captured and absorbed by a liquid film;
The tower bottom slurry oxidation section 8 comprises a tower bottom liquid collecting tank 81 with the periphery of a bottom plate connected with the inner wall of the tower body 1 and an oxidation wind distributor 83 arranged above the tower bottom liquid collecting tank 81, and the tower bottom slurry oxidation section is respectively used for storing tower bottom slurry and carrying out forced oxidation on the tower bottom slurry.
Further, the operation temperature of the integrated dedusting and desulfurizing tower is 50-65 ℃ and the operation pressure is about 3500-5000 Pa (G).
Furthermore, a plurality of inspection manholes 11, 12, 13, 14, 15, 16 are formed in the wall surface of the tower body 1 from bottom to top and are used for inspecting and maintaining components in the tower.
Further, the tower body 1 is made of an acid-resistant and wear-resistant metal material (such as 304L), a carbon steel lining acid-resistant and wear-resistant metal material (such as 304L) or a carbon steel lining nonmetal material (such as a carbon steel lining PTU), and the flue gas inlet 71 is made of an alloy material which is resistant to high temperature and acid corrosion.
Further, the bottom of the tower top chimney 2 is connected with the high-efficiency dedusting and demisting device 4 through the reducing section 3, and the reducing section 3 is in a cone shape gradually expanding downwards.
Further, a CEMS detection instrument interface 22 is arranged on the lower tower wall of the tower top chimney 2, and the distance d between the CEMS detection instrument interface 22 and the reducing section 3 is determined according to the outlet net flue gas flow and the chimney diameter. The included angle between the interface 22 of the CEMS detection instrument and the junction of the tower wall is 15-60 degrees, preferably 30-45 degrees, and is preferably arranged upwards along the horizontal direction in order to avoid the interface blockage.
Further, the flue gas inlet 71 is connected to the tower wall of the primary spraying quench section 7, and the connection angle between the flue gas inlet 71 and the tower wall is 30 ° to 90 °, preferably 60 ° to 90 °, more preferably 90 °, i.e. the flue gas inlet 71 is vertically connected to the tower wall of the primary spraying quench section 7.
Further, the quenching nozzle 72 is preferably arranged on the tower wall of the primary spraying quenching section 7 and is connected with the tower wall at a certain angle; wherein, part of the quenching spray heads 72 are arranged on the upper side and the lower side of the flue gas inlet 71 and are vertical to the direction of the flue gas inlet 71 at an angle of 90 degrees, and part of the quenching spray heads 72 are arranged on the left side and the right side of the flue gas inlet 71 and are arranged at an angle of 15 degrees to 90 degrees, preferably 15 degrees to 30 degrees, with the direction of the flue gas inlet 71. The quenching nozzle 72 is used for spraying circulating absorption slurry from the bottom of the tower to form a plurality of flat cone-shaped torrent water curtains, fully cover the whole cross section of the flue gas inlet, quench and cool the flue gas introduced into the flue gas inlet, and enable the flue gas to reach the saturation temperature. The number of quenching nozzles 72 is preferably 1 to 4, as shown in fig. 2A to 2C, that is, four quenching nozzles 72A, B, C, D are provided, wherein two quenching nozzles 72A, B are provided on the upper side and the lower side of the flue gas inlet 71, and two quenching nozzles 72C, D are provided on the left side and the right side of the flue gas inlet 71.
Further, the quench nozzle 72 may be selected from a quench nozzle disclosed in prior art CN104138812a to spray slurry to form a flat cone-shaped quench water curtain.
Further, a plurality of temperature detecting instrument interfaces 73, preferably 2-3, are arranged on the tower wall of the primary spraying quenching section 7, and are arranged at the position of the tower wall opposite to the flue gas inlet 71. The connection included angle between the temperature detection instrument interfaces 73 and the tower wall is 90 degrees, and the temperature detection instrument interfaces 73 are arranged up and down, and the interval between the interfaces is 0.5-2.0 m.
Furthermore, the secondary spraying absorption section 6 is preferably provided with 1-5 layers of absorption section spraying, and each layer of absorption section spraying is provided with 3-5 absorption section spray heads. The absorption section spray nozzles are large-caliber spray nozzles, the absorption section spray nozzles sprayed by each layer of absorption section are uniformly arranged on the same plane, and the included angle between the absorption section spray pipes and the horizontal direction is 1-10 degrees, preferably 3-6 degrees, and preferably arranged downwards along the horizontal direction. And each layer of absorption section spray head sprays slurry to form a torrent water curtain in a flat cone curtain shape to fully cover the whole cross section in the tower. As shown in fig. 3A-3B, 5 layers of absorption stage sprays 61, 62, 63, 64, 65 are provided, with 4 of said absorption stage spray heads and absorption stage spray pipes connected thereto, such as 61A, B, C, D, being provided per layer.
Furthermore, every two adjacent layers of absorption sections are sprayed and arranged in a staggered way at a certain angle, so that the jet slurry forms a torrent water curtain in a flat cone curtain shape to fully cover the cylinder body of the secondary absorption section. Specifically, the included angle of spraying in each two layers of absorption sections is 10-50 degrees, preferably 15-30 degrees. As shown in fig. 3B, the included angle of the absorption section spray between each two layers is 22.5 °.
Further, the absorption section nozzle may be selected from a quenching nozzle disclosed in prior art CN104138812a to spray slurry to form a flat cone-shaped curtain of turbulent water.
Further, a first pressure detecting instrument interface 67 is arranged on the upper tower wall of the secondary spraying absorption section 6, and an included angle between the first pressure detecting instrument interface 67 and the tower wall is 15-60 degrees, preferably 30-45 degrees, and preferably is arranged upwards along the horizontal direction.
Further, as shown in fig. 4A-4C, the bottom plate of the liquid collecting tank 51 of the dust collector is welded on the inner wall of the tower body 1 at a certain inclination angle, preferably an included angle of 10-30 ° with the horizontal direction; the bottom of the slope of the dust collector liquid collecting tank 51 is provided with a liquid storage area with a certain volume, the liquid storage height of the liquid storage area is 0.5-1.2 m, and the liquid storage area is provided with a dust collector liquid collecting tank outlet 56 towards the outer side of the wall surface of the tower body 1.
Further, the lower part of the venturi tube 52 is fixed on the bottom plate of the dust collector sump 51 by welding or flange connection; the venturi tubes 52 are fixedly connected by a rib plate. The lower end of each venturi tube 52 is connected with a guide vane segment 53, and guide vanes are arranged in the guide vane segments, so that the rising smoke gas rises in the venturi tube in a rotating way.
Further, a dust collector overflow pipe 54 is fixedly disposed through the bottom plate of the dust collector sump 51, the bottom end of the dust collector overflow pipe 54 passes through the wall surface of the tower body 1, and an overflow liquid outlet 55 is disposed.
Further, the number of the three-stage shower pipes 57 is 1 to 50, and preferably, the three-stage shower pipes are disposed at 0.5 to 1.5m at the upper end of the venturi tube 52. The inlet of the third-stage spray pipe 57 is provided with a plurality of third-stage spray pipe liquid inlets 58, which are positioned on the wall surface of the tower body 1 and connected with the outlet 56 of the liquid collecting tank of the dust collector (not shown in the figure) through a circulating pump, and the slurry collected by the liquid collecting tank 51 of the dust collector is circularly sprayed in the multi-stage spray pipe type column dust collector 5. The three-stage spray pipes 57 are downwards connected with a plurality of spray nozzles 59, each spray nozzle 59 corresponds to one venturi pipe 52, and the number of the venturi pipes 52 and the number of the spray nozzles 59 are determined according to the flow rate of the flue gas entering the tower and the components of the flue gas. As shown in fig. 4C, a total of 4 tertiary shower pipes 57 and 4 tertiary shower pipe liquid inlets 58A, B, C, D are provided.
Further, a second pressure detecting instrument interface 60 is arranged on the tower wall at the upper part of the three-stage spray multi-pipe type tube nest dust remover 5, and an included angle between the second pressure detecting instrument interface 60 and the connecting part of the tower wall is 15-60 degrees, preferably 30-45 degrees, and is preferably arranged upwards along the horizontal direction.
Further, in the high-efficiency dust-removing mist eliminator 4, the inlet of the water spray flushing pipe 42 is a spray flushing water inlet 43, which is located on the wall surface of the tower body 1 and is connected with external process water (not shown in the figure), so as to supply spray flushing water to the water spray flushing pipe 42. As shown in fig. 5A-5C, each water spraying flushing pipe 42 is connected with a plurality of water spraying hoses 45, a plurality of flushing nozzles 46 are arranged in each cyclone cylinder, and each flushing nozzle 46 is respectively connected with the water spraying flushing pipe 42 through the water spraying hose 45, so that the wall of each cyclone cylinder is wetted by spraying flushing water.
Preferably, 2 to 3 cyclone cylinders are arranged in each cyclone cylinder tube bundle 41, and 2 to 4 flushing nozzles 46 are arranged in each cyclone cylinder. The water spray rinsing pipe 42 is arranged at a position 0.5-1.2 m above the cyclone cylinder tube bundle 41.
Further, the number of cyclone tube bundles 41, the amount of spray rinsing water and the spray rinsing frequency are determined according to the flow rate of the flue gas entering the tower and the composition of the flue gas.
Further, a third pressure detecting instrument interface 47 is arranged on the tower wall at the upper part of the high-efficiency dedusting and mist-removing drip device 4, and an included angle between the third pressure detecting instrument interface 47 and the connecting part of the tower wall is 15-60 degrees, preferably 30-45 degrees, and is preferably arranged upwards along the horizontal direction.
Further, as shown in fig. 6A-6B, the bottom plate of the bottom sump 81 is welded to the inner wall of the tower body 1 at a certain inclination angle, preferably an angle of 15 ° to 60 °, more preferably 15 ° to 30 °, with respect to the horizontal direction. The bottom of the slope of the tower bottom liquid collecting tank 81 is provided with a tower bottom slurry outlet 82 towards the outer side of the wall surface of the tower body 1, and the tower bottom slurry outlet 82 is connected with the quenching spray pipe 74 and the absorption section spray pipe (not shown in the figure) through a circulating pump to provide circulating slurry for spraying in the primary spraying quenching section 7 and the secondary spraying absorption section 6.
Further, the inlet of the oxidation wind distributor 83 is provided with a plurality of oxidation wind inlets 84, which are located on the wall surface of the tower body 1 and connected with an external oxidation fan (not shown in the figure). The relative distance between the oxidation wind distributor 83 and the bottom plate of the tower body 1 is determined according to the liquid level height of the liquid stored in the tower bottom slurry oxidation section 8, and the distance between the oxidation wind distributor 83 and the bottom plate of the tower body 1 is generally 0.5-2.0 m; the distance from the level of the stored liquid is 5 to 10m, preferably 6 to 8m.
Further, the oxidation wind distributor 83 includes a plurality of oxidation wind main pipes and a plurality of oxidation wind branch pipes, a plurality of wind outlet holes 87 are equidistantly formed on the oxidation wind branch pipes, the diameter of each wind outlet hole 87 is 50-150 mm, and the distance between every two adjacent wind outlet holes 87 is 0.5-800 mm. The number of the main oxidized wind pipes and the branch oxidized wind pipes is determined according to the smoke components in the tower and the concentration of sulfite contained in absorption slurry.
Further, a bottom oxidizing liquid return pipe 86 is arranged above the bottom plate of the bottom liquid collecting tank 81 near the bottom plate, the oxidizing liquid return pipe 86 is arc-shaped and is arranged along the wall surface of the tower body 1, and a plurality of liquid outlet holes 89 are formed on the bottom oxidizing liquid return pipe 86 at equal intervals for flushing the bottom plate of the bottom liquid collecting tank 81 by slurry return; the diameter of the liquid outlet holes 89 is 50-200 mm, and the distance between the adjacent liquid outlet holes 89 is 0.56-1.2 m.
Further, an overflow port 88 and a tower returning slurry inlet 85 are also arranged on the tower wall of the tower bottom slurry oxidation section 8. The return slurry inlet 85 communicates with the overflow outlet 55 (not shown) for circulating slurry in the three stage spray multi-tube stack scrubber 5 to the bottom slurry oxidation stage 8 via overflow.
The present application has been described in detail with the purpose of enabling those skilled in the art to understand the contents of the present application and to implement the same, but not to limit the scope of the present application, and all equivalent changes or modifications made according to the spirit of the present application should be covered in the scope of the present application.
Claims (10)
1. Novel catalytic cracking flue gas integration dust removal desulfurizing tower, a serial communication port, integration dust removal desulfurizing tower includes the tower body, set gradually overhead chimney, reducing section, high-efficient dust removal defogging drip ware, tertiary spraying multitube row Guan Chuchen ware, second grade spray absorption section, one-level spray quench section and tower bottom thick liquid oxidation section from top to bottom on the tower body, the top of overhead chimney sets up the purification flue gas export, one-level spray quench section sets up the flue gas import, wherein:
a plurality of quenching spray heads are arranged on the tower wall of the primary spraying quenching section or the flue gas inlet;
the secondary spraying absorption section comprises a plurality of layers of absorption section spraying from bottom to top, and each layer of absorption section spraying is provided with a plurality of absorption section spray heads;
The three-stage spray multi-tube type tube nest dust remover comprises a dust remover liquid collecting tank, a plurality of parallel venturi tubes and a three-stage spray tube, wherein the periphery of the bottom plate of the dust remover liquid collecting tank is connected with the inner wall of the tower body;
The efficient dedusting and mist-removing drip catcher comprises a plurality of cyclone cylinder tube bundles which are arranged in parallel and a plurality of water spraying flushing pipes which are arranged above the cyclone cylinder tube bundles, wherein the cyclone cylinder tube bundles comprise a plurality of cyclone cylinders, and cyclone plates are arranged in the cyclone cylinders.
2. The integrated dust removal and desulfurization tower according to claim 1, wherein the operation temperature of the integrated dust removal and desulfurization tower is 50-65 ℃ and the operation pressure is 3500-5000 Pa (G); the tower body is made of an acid-resistant and wear-resistant metal material, a carbon steel lining acid-resistant and wear-resistant metal material or a carbon steel lining nonmetal material, and the smoke inlet is made of a high-temperature-resistant and acid-resistant alloy material.
3. The integrated dedusting and desulfurizing tower according to claim 1, wherein in the primary spray quench section, the flue gas inlet is connected with the tower wall of the primary spray quench section, and the connection included angle with the tower wall is 30-90 degrees, preferably 60-90 degrees, more preferably 90 degrees;
The quenching spray head is arranged on the tower wall of the primary spraying quenching section and is connected with the tower wall at a certain angle; wherein, part of quenching spray heads are arranged on the upper side and the lower side of the flue gas inlet and are vertical to the direction of the flue gas inlet at an angle of 90 degrees, and part of quenching spray heads are arranged on the left side and the right side of the flue gas inlet and are arranged at an angle of 15 degrees to 90 degrees, preferably 15 degrees to 30 degrees, with the direction of the flue gas inlet.
4. The integrated dedusting and desulfurizing tower according to claim 1, wherein in the secondary spraying absorption section, 1-5 layers of absorption section spraying are arranged, 3-5 absorption section spray heads are arranged on each layer of absorption section spraying, and the absorption section spray heads of each layer are uniformly arranged on the same plane;
an absorption section spray pipe connected with the inlet of the absorption section spray head is connected with the tower wall of the secondary spraying absorption section, and the absorption section spray pipe is downwards arranged along the horizontal direction, and the included angle between the absorption section spray pipe and the horizontal direction is 1-10 degrees, preferably 3-6 degrees;
the spraying of each two adjacent layers of absorption sections is in staggered arrangement at a certain angle, and the included angle of the spraying of each two layers of absorption sections is 10-50 degrees, preferably 15-30 degrees.
5. The integrated dedusting and desulfurizing tower according to claim 1, wherein in the three-stage spray multitube type tube nest deduster, the lower part of the venturi tube is fixed on the bottom plate of the deduster liquid collecting tank through welding or flange connection; the venturi tubes are fixedly connected through rib plates; the lower end of each venturi tube is connected with a guide vane segment, and guide vanes are arranged in the venturi tube;
the bottom plate of the dust collector liquid collecting tank is fixedly provided with a dust collector overflow pipe, the bottom end of the dust collector overflow pipe penetrates through the wall surface of the tower body, and an overflow liquid outlet is arranged.
6. The integrated dust removal and desulfurization tower according to claim 1, wherein a bottom plate of the dust collector liquid collection tank is welded on the inner wall of the tower body at an inclined angle of 10-30 degrees with the horizontal direction; a liquid storage area is arranged at the slope bottom of the dust collector liquid collecting tank, and a dust collector liquid collecting tank outlet is formed in the liquid storage area towards the outer side of the wall surface of the tower body;
The three-stage spray pipes are downwards connected with a plurality of spray nozzles, and each spray nozzle corresponds to one venturi pipe; the inlet of the third-stage spray pipe is provided with a plurality of third-stage spray pipe liquid inlets which are positioned on the wall surface of the tower body and are connected with the outlet of the liquid collecting tank of the dust remover through a circulating pump;
The number of the three-stage spray pipes is 1-50, and the three-stage spray pipes are arranged at 0.5-1.5 m at the upper end of the venturi pipe.
7. The integrated dedusting and desulfurizing tower according to claim 1, wherein in the high-efficiency dedusting and mist-droplet removing device, each water spray flushing pipe is connected with a plurality of water spray hoses, a plurality of flushing nozzles are arranged in each cyclone cylinder, and each flushing nozzle is connected with the water spray flushing pipe through the water spray hose;
2-3 cyclone cylinders are arranged in each cyclone cylinder tube bundle, and 2-4 flushing nozzles are arranged in each cyclone cylinder; and the water spraying flushing pipe is arranged at a position 0.5-1.2 m above the cyclone cylinder tube bundle.
8. The integrated dedusting and desulfurizing tower according to claim 1, wherein the tower bottom slurry oxidation section comprises a tower bottom liquid collecting tank with the periphery of a bottom plate connected with the inner wall of the tower body and an oxidation wind distributor arranged above the tower bottom liquid collecting tank;
The bottom plate of the tower bottom liquid collecting tank is welded on the inner wall of the tower body at an inclined angle of 15-60 degrees with the horizontal direction, preferably 15-30 degrees;
The bottom plate top of tower bottom collecting tank sets up the tower bottom oxidation liquid back flow, the oxidation liquid back flow is the arc and sets up along the wall of tower body, the equidistance leaves on the tower bottom oxidation liquid back flow and is equipped with a plurality of drain holes.
9. The integrated dedusting and desulfurizing tower according to claim 8, wherein the inlet of the oxidation wind distributor is provided with a plurality of oxidation wind inlets which are positioned on the wall surface of the tower body and are connected with an external oxidation fan;
The oxidation wind distributor comprises a plurality of oxidation wind main pipes and a plurality of oxidation wind branch pipes, and a plurality of wind outlet holes are formed in the oxidation wind branch pipes at equal intervals;
The distance between the oxidation wind distributor and the bottom plate of the tower body is 0.5-2.0 m, and the distance between the oxidation wind distributor and the liquid level height of the stored liquid is 5-10 m, preferably 6-8 m.
10. The integrated dedusting and desulfurizing tower according to claim 1, wherein a plurality of temperature detection instrument interfaces are arranged on the tower wall of the primary spraying quenching section and are arranged at the position of the tower wall opposite to the flue gas inlet, the connection included angle between the temperature detection instrument interfaces and the tower wall is 90 degrees, the temperature detection instrument interfaces are arranged up and down, and the interval between the interfaces is 0.5-2.0 m;
the upper tower wall of the secondary spray absorption section, the tower wall of the upper part of the three-stage spray multi-pipe type tube nest dust remover and the tower wall of the upper part of the high-efficiency dust and mist remover are respectively provided with a pressure detection instrument interface, and the lower tower wall of the tower top chimney is provided with a CEMS detection instrument interface; the instrument interfaces are all arranged upwards along the horizontal direction, and the included angle between the instrument interfaces and the junction of the tower wall is 15-60 degrees, preferably 30-45 degrees.
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| CN202410253460.9A CN118059666A (en) | 2024-03-06 | 2024-03-06 | Novel catalytic cracking flue gas integrated dust removal desulfurizing tower |
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| CN202410253460.9A CN118059666A (en) | 2024-03-06 | 2024-03-06 | Novel catalytic cracking flue gas integrated dust removal desulfurizing tower |
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