CN218290447U - Waste sulfuric acid cracking regeneration system - Google Patents
Waste sulfuric acid cracking regeneration system Download PDFInfo
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- CN218290447U CN218290447U CN202121241118.5U CN202121241118U CN218290447U CN 218290447 U CN218290447 U CN 218290447U CN 202121241118 U CN202121241118 U CN 202121241118U CN 218290447 U CN218290447 U CN 218290447U
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Abstract
The utility model relates to a waste sulfuric acid recovery processing technical field, concretely relates to waste sulfuric acid schizolysis regeneration system, handle the workshop section including schizolysis workshop section, purification workshop section, conversion workshop section, dry-suction workshop section and tail gas. The cracking section cracks the waste sulfuric acid through high-temperature combustion to generate cracking flue gas, the purification section purifies the cracking flue gas to remove most of dust and harmful components in the flue gas, the cracking flue gas passing through the purification section further enters the conversion section to catalyze sulfur dioxide therein into sulfur trioxide at a high temperature through catalysis, and the sulfur trioxide is conveyed to the dry absorption section to be absorbed, so that sulfuric acid is produced, and the efficient regeneration of the waste sulfuric acid is realized. In addition, sulfur dioxide in the flue gas which passes through the dry absorption section and is not converted and absorbed is treated again through the tail gas treatment working section, so that the content of the sulfur dioxide in the vented flue gas is further reduced, and the environmental protection is facilitated.
Description
Technical Field
The utility model relates to a waste sulfuric acid recovery processing technical field especially relates to a waste sulfuric acid schizolysis regeneration system.
Background
In industrial production in China, waste sulfuric acid is mainly derived from the production processes of pesticides, ammonium sulfate, calcium superphosphate, titanium dioxide and petroleum industry gasoline lubricating oil; the processes of nitration, sulfonation, esterification alkylation, catalysis, drying and the like of organic matters; steel pickling, gas drying and the like. The waste sulfuric acid is diluted and polluted in the using process, so that the waste sulfuric acid can not be directly used again. How to properly treat and recover the waste sulfuric acid becomes an urgent problem to be solved, and the current waste acid treatment methods mainly comprise 3 types, namely waste sulfuric acid concentration, waste sulfuric acid purification and waste sulfuric acid cracking regeneration.
When the waste sulfuric acid can not be concentrated and purified, the cracking regeneration treatment of the waste sulfuric acid can be selected, and the cracking regeneration of the waste sulfuric acid can produce qualified industrial-grade concentrated sulfuric acid. The sulfuric acid contains 32.6% of sulfur, the waste sulfuric acid can also be used as a raw material for producing sulfuric acid, the waste sulfuric acid treatment device is not only an environment-friendly device, but also a sulfuric acid production device, the raw material has no cost, a new industrial grade product sulfuric acid regenerated by cracking waste acid can be used by enterprises, and meanwhile, the pollution problem of the enterprises is also solved. The sulfur dioxide recovery rate of the commonly used waste sulfuric acid cracking regeneration system in the prior art is low, so that the content of sulfur dioxide in the exhaust flue gas is high, the environment protection is not facilitated, and the economic benefit of the waste sulfuric acid cracking regeneration system is poor.
SUMMERY OF THE UTILITY MODEL
For solving the technical problem, an object of the utility model is to provide a waste sulfuric acid schizolysis regeneration system, waste sulfuric acid schizolysis regeneration system handles the recovery through the schizolysis flue gas that carries out the schizolysis and produce after the schizolysis to regeneration is carried out waste sulfuric acid, and regeneration efficiency is higher.
In order to achieve the technical effects, the utility model adopts the following technical scheme:
a waste sulfuric acid cracking regeneration system comprises a cracking section, a purification section, a conversion section, a dry absorption section and a tail gas treatment section, wherein the cracking section comprises a waste acid cracking furnace, the waste acid cracking furnace is connected with a combustion-supporting gas preheating unit, the waste acid cracking furnace is provided with a first flue gas outlet, and the first flue gas outlet is connected with the purification section; a second flue gas outlet is formed in the purification working section and connected with the dry absorption working section; the dry absorption working section comprises a drying tower and an absorption tower, the drying tower is connected with the purification working section, a third flue gas outlet is formed in the drying tower, and the third flue gas outlet is connected with the conversion working section; the conversion section comprises a heat exchange unit and a converter arranged at the downstream of the heat exchange unit, a multi-section catalytic packing layer is sequentially arranged in the converter from top to bottom, a fourth flue gas outlet is arranged on the converter, and the fourth flue gas outlet is connected with the absorption tower; the absorption tower is connected with a tail gas treatment working section; the tail gas treatment section comprises a desulfurizing tower, a desorption tower and a tail gas treatment unit which are sequentially connected, a discharge chimney is arranged at the top of the desulfurizing tower, a fifth flue gas outlet is arranged on the desorption tower, and the fifth flue gas outlet is connected with the tail gas treatment unit.
Furthermore, a first spraying mechanism is arranged at the top of the drying tower, a second spraying mechanism is arranged at the top of the absorption tower, and the first spraying mechanism and the second spraying mechanism are used for spraying acid liquor.
Further, combustion-supporting gas preheats the unit including the one-level air heater and the second grade air heater who connects gradually, the one-level air heater is connected with the air-blower just the second grade air heater pass through air conveying pipeline with spent acid pyrolysis furnace intercommunication.
Furthermore, a waste heat boiler is further arranged at the first smoke outlet and connected with the combustion-supporting gas waste heat unit.
Furthermore, a waste acid spray gun is arranged on the waste acid cracking furnace, and a compressed air spray pipe communicated with the waste acid spray gun is further arranged on the waste acid spray gun.
Further, the purification section comprises a dynamic wave washing tower, a filler washing tower and an electric demister which are sequentially connected, wherein the dynamic wave washing tower is connected with the first flue gas outlet, and the second flue gas outlet is fixedly connected with the electric demister.
Further, the dry absorption section further comprises a dilute acid circulation tank and a concentrated acid circulation tank, the drying tower is connected with the dilute acid circulation tank through a first acid conveying pipeline, the absorption tower is connected with the concentrated acid circulation tank through a second acid conveying pipeline, a third acid conveying pipeline is further arranged between the concentrated acid circulation tank and the dilute acid circulation tank, an outer discharge pipeline is further arranged on the concentrated acid circulation tank, and an acid plate type cooler is arranged on the outer discharge pipeline.
Further, the heat exchange unit comprises a four-section gas-gas heat exchanger, a three-section gas-gas heat exchanger, a two-section gas-gas heat exchanger and a one-section gas-gas heat exchanger which are sequentially connected, the four-section gas-gas heat exchanger is connected with a third flue gas outlet, the one-section gas-gas heat exchanger is connected with the converter, and an electric heating furnace is further arranged between the one-section gas-gas heat exchanger and the converter.
Furthermore, the bottom of the desulfurizing tower is provided with a first liquid storage area, the bottom of the desorption tower is provided with a second liquid storage area, the desulfurizing tower is connected with the desorption tower through a lean-rich liquid heat exchanger, and the desorption tower is further connected with a steam reboiler.
Furthermore, a sixth flue gas outlet is formed in the desorption tower, the tail gas treatment unit comprises a gas-liquid separator connected with the sixth flue gas outlet, a seventh flue gas outlet is formed in the gas-liquid separator, and the seventh flue gas outlet is communicated with the drying tower.
Compared with the prior art, the beneficial effects of the utility model are that: the utility model provides a pair of waste sulfuric acid schizolysis regeneration system includes schizolysis workshop section, purification workshop section, conversion workshop section, dry absorption workshop section and tail gas treatment workshop section, wherein, thereby the schizolysis workshop section carries out the schizolysis to waste sulfuric acid through high temperature combustion and produces the schizolysis flue gas, and purification workshop section then carries out purification treatment to the schizolysis flue gas in order to detach most dust and harmful component in the flue gas, and the schizolysis flue gas through purification workshop section further gets into the conversion workshop section and catalyzes sulfur dioxide wherein for sulfur trioxide and carry to the dry absorption workshop section and absorb through catalysis under higher temperature to production sulfuric acid realizes the high-efficient regeneration of waste sulfuric acid. In addition, sulfur dioxide in the flue gas which passes through the dry absorption section and is not converted and absorbed is treated again by the tail gas treatment section, so that the content of the sulfur dioxide in the vented flue gas is further reduced, and the environmental protection is facilitated.
Drawings
Fig. 1 is a schematic diagram of an overall structure of a waste sulfuric acid cracking and regenerating system according to an embodiment of the present invention;
the reference signs are: 10, a waste acid cracking furnace, 11, a natural gas pipeline, 12, a waste acid spray gun, 121, a compressed air spray pipe, 13, an air conveying pipeline, 131, a primary air preheater, 132, a secondary air preheater, 14, a waste heat boiler, 21, a dynamic wave washing tower, 22, a packing washing tower, 23, an electric demister, 31, a drying tower, 311, a dilute acid circulating tank, 32, an absorption tower, 321, a concentrated acid circulating tank, 331, a first acid conveying pipeline, 332, a second acid conveying pipeline, 333, a third acid conveying pipeline, 41, a four-section gas-gas heat exchanger, 42, a three-section gas-gas heat exchanger, 43, a two-section gas-gas heat exchanger, 44, a one-section gas-gas heat exchanger, 441, an electric heating furnace, 45, a converter, 451, a one-section catalyst, 452, a two-section catalyst, 453, a three-section catalyst, 454, a four-section catalyst, 51, a desulfurizing tower, 52, a desorption tower, 53, a lean-rich liquid heat exchanger, 531, a lean liquid recooler, 54, a steam reboiler, 55, and a gas-liquid separator.
Detailed Description
Embodiments of the present invention will be described in detail with reference to the accompanying drawings. The following examples are only for illustrating the technical solutions of the present invention more clearly, and therefore are only examples, and the protection scope of the present invention is not limited thereby.
As shown in fig. 1, the system for cracking and regenerating waste sulfuric acid provided in this embodiment includes a cracking section, a purification section, a conversion section, a dry absorption section, and a tail gas treatment section.
In this embodiment, the cracking section includes a spent acid cracking furnace 10, the spent acid cracking furnace 10 is connected with a combustion-supporting gas preheating unit, a first flue gas outlet is arranged on the spent acid cracking furnace 10, and the first flue gas outlet is connected with the purification section. Specifically, a natural gas pipeline 11 and a waste acid spray gun 12 are arranged on the waste acid cracking furnace 10, the natural gas pipeline 11 is used for conveying natural gas, and a compressed air spray pipe 121 communicated with the waste acid spray gun 12 is arranged on the waste acid spray gun 12. The combustion-supporting gas preheats the unit including the one-level air heater 131 and the second grade air heater 132 that connect gradually, one-level air heater 131 is connected with the air-blower just second grade air heater 132 pass through air conveying pipeline 13 with spent acid pyrolysis furnace 10 intercommunication. A waste heat boiler 14 is further arranged at the first flue gas outlet, and the waste heat boiler 14 is connected with the secondary air preheater 132. In the specific implementation, the waste sulfuric acid is sent into a waste acid spray gun 12 matched with the waste acid cracking furnace 10 through a waste acid pump, the waste acid spray gun 12 is fully mixed with the compressed air in the compressed air spray pipe 121 and atomized and sprayed into the waste acid cracking furnace 10, meanwhile, the natural gas and the air preheated by the primary air preheater 131 and the secondary air preheater 132 in the waste acid cracking furnace 10 are fully mixed and combusted, the high temperature generated by combustion reaches 1000-1200 ℃, the waste sulfuric acid is completely cracked at the high temperature, and the hexavalent sulfate radicals in the waste sulfuric acid are completely reduced to sulfur dioxide. During implementation, an oxygen meter can be adopted to control the oxygen concentration at the outlet of the waste acid cracking furnace 10, so that the oxygen concentration is controlled to be 2-5%, and the temperature of the waste acid cracking furnace 10 is controlled to be about 1150 ℃ so that the waste acid is fully cracked. The temperature of sulfur dioxide flue gas at the outlet of the waste acid cracking furnace 10 is reduced to-600 ℃ after being cooled by a waste heat boiler 14, the sulfur dioxide flue gas enters a secondary air preheater 132 to heat air from a primary air preheater 131, the air is heated to about 500 ℃, the temperature of the flue gas is reduced to-350 ℃, and the flue gas discharged from the primary air preheater 131 is sent to a purification working section.
In this embodiment, the purification section is provided with a second flue gas outlet, the second flue gas outlet is connected with the dry absorption section, specifically, the purification section includes a dynamic wave washing tower 21, a filler washing tower 22 and an electric demister 23, which are connected in sequence, the dynamic wave washing tower 21 is connected with the first flue gas outlet, and the second flue gas outlet is fixedly connected with the electric demister 23. In the specific implementation, the flue gas of about 350 ℃ delivered by the primary air preheater 131 of the self-cracking section enters the reverse spray pipe of the dynamic wave washing tower 21 from the upper part of the dynamic wave washing tower 21, and collides and contacts with the washing liquid (the washing liquid is dilute sulfuric acid with the concentration of about 5%) sprayed into the reverse spray pipe of the dynamic wave washing tower 21 from bottom to top at high speed to form a foam layer, so that the cracked flue gas generated by cracking the waste sulfuric acid is fully washed to remove most of dust and harmful components in the flue gas, and meanwhile, the cracked flue gas is subjected to heat insulation humidification and temperature reduction to about 80 ℃ in the dynamic wave washing tower 21. And the cooled flue gas enters a filler washing tower 22 for further cooling and dedusting, the temperature of the flue gas is reduced to about 40 ℃, and finally acid mist water mist is removed by an electric demister 23, so that the acid mist content in the cracked flue gas at the second flue gas outlet is less than 30mg/Nm & lt 3 & gt. The purified flue gas is continuously sent to the dry-suction working section through a second flue gas outlet.
In this embodiment, the dry absorption section includes a drying tower 31 and an absorption tower 32, the drying tower 31 is connected to the purification section, and a third flue gas outlet is provided on the drying tower 31 and connected to the conversion section. The drying tower comprises a drying tower 31, and is characterized in that a first spraying mechanism is arranged at the top of the drying tower 31, a second spraying mechanism is arranged at the top of an absorption tower 32, a first packing layer and a second packing layer are respectively arranged below the first spraying mechanism and the second spraying mechanism, and the first spraying mechanism and the second spraying mechanism are used for spraying acid liquor. The first spraying mechanism is used for spraying a dilute acid solution which is 93% concentrated sulfuric acid, and the second spraying mechanism is used for spraying 98% concentrated sulfuric acid to absorb sulfur trioxide. Specifically, the dry absorption section further comprises a dilute acid circulation tank 311 and a concentrated acid circulation tank 321, the drying tower 31 is connected with the dilute acid circulation tank 311 through a first acid conveying pipeline 331, the absorption tower 32 is connected with the concentrated acid circulation tank 321 through a second acid conveying pipeline 332, and a third acid conveying pipeline 333 is further arranged between the concentrated acid circulation tank 321 and the dilute acid circulation tank 311. In specific implementation, the cracked flue gas from the purification section is sent to the lower part of the drying tower 31 through the second flue gas outlet, the cracked flue gas is in full contact with 93% concentrated sulfuric acid sprayed from the top of the drying tower 31 in the first packing layer so as to absorb moisture in the cracked flue gas, and the moisture content of the cracked flue gas after drying is below 0.1g/Nm & lt 3 & gt. Meanwhile, during implementation, a certain amount of air can be supplemented into the drying tower 31, the oxygen-sulfur ratio in the pyrolysis flue gas is controlled to be about 1.3, the concentration of sulfur dioxide in the pyrolysis flue gas is adjusted to be more than 6%, and then the flue gas is conveyed to the conversion section through a third flue gas outlet.
In specific implementation, the conversion section includes a heat exchange unit and a converter 45 disposed at the downstream of the heat exchange unit, a multi-section catalytic packing layer is sequentially disposed in the converter 45 from top to bottom, and the multi-section catalytic packing layer sequentially includes a first section of catalyst 451, a second section of catalyst 452, a third section of catalyst 453, and a fourth section of catalyst 454 from top to bottom. The heat exchange unit comprises a four-section gas-gas heat exchanger 41, a three-section gas-gas heat exchanger 42, a two-section gas-gas heat exchanger 43 and a one-section gas-gas heat exchanger 44 which are sequentially connected, the four-section gas-gas heat exchanger 41 is connected with a third flue gas outlet, the one-section gas-gas heat exchanger 44 is connected with a converter 45, and an electric heating furnace 441 is further arranged between the one-section gas-gas heat exchanger 44 and the converter 45. In specific implementation, flue gas from the dry absorption section and dried by the drying tower 31 enters a sulfur dioxide blower to be pressurized, then passes through the four-section gas-gas heat exchanger 41, the three-section gas-gas heat exchanger 42, the two-section gas-gas heat exchanger 43 and the one-section gas-gas heat exchanger 44 in sequence to exchange heat and raise the temperature, and is heated by the electric heating furnace 441 to keep the temperature of the flue gas at about 420 ℃ and then enters the converter 45. The sulfur dioxide flue gas is converted into sulfur trioxide gas through the catalytic action of the first-stage catalyst 451, the second-stage catalyst 452, the third-stage catalyst 453 and the fourth-stage catalyst 454 in the converter 45 in sequence, so that the total conversion rate of the sulfur dioxide can reach 97.8%. In the converter 45, in order to make the flue gas temperature meet the inlet temperature requirement of each section of catalyst, inlets of the first section of catalyst 451, the second section of catalyst 452, the third section of catalyst 453 and the fourth section of catalyst 454 are connected with a gas-gas heat exchanger through pipelines, so that the flue gas exchanges heat with the dried sulfur dioxide flue gas, and the conversion efficiency of the converter is improved.
In this embodiment, the converter 45 is provided with a fourth flue gas outlet, and the fourth flue gas outlet is connected with the absorption tower 32. When the method is specifically implemented, after sulfur dioxide flue gas is converted into sulfur trioxide flue gas in the conversion working section, the temperature of the sulfur trioxide flue gas is reduced to about 180 ℃ through heat exchange of the four-section gas-gas heat exchanger 41, the sulfur trioxide flue gas is sent back to the dry absorption working section again and enters the absorption tower 32, the sulfur trioxide flue gas enters the absorption tower 32 from the bottom of the absorption tower 32, the sulfur trioxide flue gas is fully contacted with 98% concentrated sulfuric acid sprayed from the top of the absorption tower 32 at the second packing layer, the sulfur trioxide in the flue gas is fully absorbed, and the absorption rate can reach 99.99%. The top of the absorption tower 32 is also provided with a tower top demister, and flue gas enters a tail gas treatment section after being demisted by the tower top demister. Meanwhile, after further absorbing sulfur trioxide, 98% concentrated sulfuric acid is conveyed to a concentrated acid circulation tank 321, an outer discharge pipeline is further arranged on the concentrated acid circulation tank 321, and an acid plate type cooler is arranged on the outer discharge pipeline. In specific implementation, the concentrated acid circulation tank 321 is diluted by adding water to adjust the acid concentration to 98%, and then the concentrated acid circulation tank is pumped into an acid plate cooler through an absorption tower 32 circulation pump to be cooled, and then the concentrated acid can further enter the absorption tower 32 for recycling, or a part of the concentrated acid can be connected in series with the dilute acid circulation tank 311 to improve the concentrated acid concentration in the dilute acid circulation tank 311, and in addition, the concentrated acid can be sent to a finished product acid storage tank for storage through the discharge pipeline.
In this embodiment, the tail gas treatment section includes a desulfurization tower 51, a desorption tower 52 and a tail gas treatment unit, which are connected in sequence, and a fifth flue gas outlet is arranged on the desorption tower 52, and is connected with the tail gas treatment unit. The bottom of the desulfurizing tower 51 is provided with a first liquid storage area, the bottom of the desorption tower 52 is provided with a second liquid storage area, the desulfurizing tower 51 is connected with the desorption tower 52 through a lean rich liquid heat exchanger 53, and the desorption tower 52 is further connected with a steam reboiler 54. The top of the desulfurizing tower 51 is provided with a discharge chimney, and the absorption tower 32 is connected with a tail gas treatment section. Specifically, a sixth flue gas outlet is arranged on the desorption tower 52, the tail gas treatment unit comprises a gas-liquid separator 55 connected with the sixth flue gas outlet, a seventh flue gas outlet is arranged on the gas-liquid separator 55, and the seventh flue gas outlet is communicated with the drying tower 31. In specific implementation, the flue gas from the dry absorption section and absorbed by the absorption tower 32 further enters the desulfurizing tower 51, the temperature of the tail gas entering the desulfurizing tower 51 is about 80 ℃, the flue gas is in countercurrent contact with the organic amine desulfurizing agent sprayed from the top of the tower in the desulfurizing tower 51 to remove sulfur dioxide in the flue gas, the desulfurization rate reaches 99.99%, and the flue gas after desulfurization is discharged from a discharge chimney of the desulfurizing tower 51. And the organic amine rich solution in the desulfurizing tower 51 enters a first liquid storage area and is sent into a lean and rich solution heat exchanger 53 through a rich solution pump, the rich solution is preheated and then enters a desorption tower 52 to desorb sulfur dioxide gas absorbed in the rich solution, the desorption temperature is controlled to be about 100 ℃, a heat source is supplied from low-pressure saturated steam outside a steam reboiler 54, the organic amine rich solution is desorbed and then becomes organic amine lean solution, the organic amine lean solution reaches a second liquid storage area, the organic amine rich solution is sent into the lean and rich solution heat exchanger 53 through a lean solution pump, the rich solution is firstly heated, then is cooled to about 40 ℃ through a lean solution recooler 531 and then enters the top of the desulfurizing tower 51 to be sprayed to absorb sulfur dioxide in tail gas again. The sulfur dioxide gas analyzed from the top of the desorption tower 52 and the water vapor enter the gas-liquid separator 55 together for gas-liquid separation, the separated gas is mainly sulfur dioxide gas, the sulfur dioxide gas is sent back to the inlet end of the drying tower 31 of the dry absorption section, and the gas and the sulfur dioxide flue gas from the purification section are used as feed gas to be dried in the drying tower 31 and then converted and absorbed again, so that the sulfur resource can be fully utilized, and the standard emission of the sulfur dioxide flue gas is facilitated.
Although the present invention has been described in detail with reference to the preferred embodiments, those skilled in the art will understand that the technical solutions of the present invention can be modified or replaced with other equivalents without departing from the spirit and scope of the technical solutions of the present invention, which should be covered by the scope of the claims of the present invention. The technology, shape and construction parts which are not described in detail in the present invention are known technology.
Claims (10)
1. The utility model provides a waste sulfuric acid schizolysis regeneration system which characterized in that, includes schizolysis workshop section, purification workshop section, conversion workshop section, dry absorption workshop section and tail gas treatment workshop section, wherein: the waste acid cracking process comprises a waste acid cracking furnace (10), wherein the waste acid cracking furnace (10) is connected with a combustion-supporting gas preheating unit, a first flue gas outlet is formed in the waste acid cracking furnace (10), and the first flue gas outlet is connected with a purification process; a second flue gas outlet is formed in the purification working section and connected with the dry absorption working section; the dry absorption section comprises a drying tower (31) and an absorption tower (32), the drying tower (31) is connected with the purification section, a third flue gas outlet is formed in the drying tower (31), and the third flue gas outlet is connected with the conversion section; the conversion section comprises a heat exchange unit and a converter (45) arranged at the downstream of the heat exchange unit, a plurality of sections of catalytic packing layers are sequentially arranged in the converter (45) from top to bottom, a fourth flue gas outlet is arranged on the converter (45), and the fourth flue gas outlet is connected with the absorption tower (32); the absorption tower (32) is connected with a tail gas treatment working section; the tail gas treatment section comprises a desulfurizing tower (51), a desorption tower (52) and a tail gas treatment unit which are sequentially connected, a discharge chimney is arranged at the top of the desulfurizing tower (51), a fifth flue gas outlet is arranged on the desorption tower (52), and the fifth flue gas outlet is connected with the tail gas treatment unit.
2. The spent sulfuric acid cracking regeneration system of claim 1, wherein: the top of the drying tower (31) is provided with a first spraying mechanism, the top of the absorption tower (32) is provided with a second spraying mechanism, and the first spraying mechanism and the second spraying mechanism are used for spraying acid liquor.
3. The spent sulfuric acid cracking regeneration system of claim 1, wherein: the combustion-supporting gas preheating unit comprises a primary air preheater (131) and a secondary air preheater (132) which are sequentially connected, wherein the primary air preheater (131) is connected with an air blower, and the secondary air preheater (132) is communicated with the waste acid cracking furnace (10) through an air conveying pipeline (13).
4. The spent sulfuric acid cracking regeneration system of claim 1, wherein: and a waste heat boiler (14) is further arranged at the first flue gas outlet, and the waste heat boiler (14) is connected with the combustion-supporting gas waste heat unit.
5. The spent sulfuric acid cracking regeneration system of claim 1, wherein: a waste acid spray gun (12) is arranged on the waste acid cracking furnace (10), and a compressed air spray pipe (121) communicated with the waste acid spray gun (12) is further arranged on the waste acid spray gun (12).
6. The spent sulfuric acid cracking regeneration system of claim 1, wherein: the purification working section comprises a dynamic wave washing tower (21), a filler washing tower (22) and an electric demister (23) which are sequentially connected, wherein the dynamic wave washing tower (21) is connected with a first flue gas outlet, and a second flue gas outlet is fixedly connected with the electric demister (23).
7. The spent sulfuric acid cracking regeneration system of claim 1, wherein: the drying and absorbing section further comprises a dilute acid circulating tank (311) and a concentrated acid circulating tank (321), the drying tower (31) is connected with the dilute acid circulating tank (311) through a first acid conveying pipeline (331), the absorbing tower (32) is connected with the concentrated acid circulating tank (321) through a second acid conveying pipeline (332), a third acid conveying pipeline (333) is further arranged between the concentrated acid circulating tank (321) and the dilute acid circulating tank (311), an outer discharging pipeline is further arranged on the concentrated acid circulating tank (321), and an acid plate type cooler is arranged on the outer discharging pipeline.
8. The spent sulfuric acid cracking regeneration system of claim 1, wherein: the heat exchange unit comprises a four-section gas-gas heat exchanger (41), a three-section gas-gas heat exchanger (42), a two-section gas-gas heat exchanger (43) and a one-section gas-gas heat exchanger (44) which are sequentially connected, the four-section gas-gas heat exchanger (41) is connected with a third flue gas outlet, the one-section gas-gas heat exchanger (44) is connected with a converter (45), and an electric heating furnace (441) is further arranged between the one-section gas-gas heat exchanger (44) and the converter (45).
9. The spent sulfuric acid cracking regeneration system of claim 1, wherein: the bottom of the desulfurizing tower (51) is provided with a first liquid storage area, the bottom of the desorption tower (52) is provided with a second liquid storage area, the desulfurizing tower (51) is connected with the desorption tower (52) through a lean and rich liquid heat exchanger (53), and the desorption tower (52) is further connected with a steam reboiler (54).
10. The system of claim 1, wherein: a sixth flue gas outlet is formed in the desorption tower (52), the tail gas treatment unit comprises a gas-liquid separator (55) connected with the sixth flue gas outlet, a seventh flue gas outlet is formed in the gas-liquid separator (55), and the seventh flue gas outlet is communicated with the drying tower (31).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121241118.5U CN218290447U (en) | 2021-06-04 | 2021-06-04 | Waste sulfuric acid cracking regeneration system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121241118.5U CN218290447U (en) | 2021-06-04 | 2021-06-04 | Waste sulfuric acid cracking regeneration system |
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| CN218290447U true CN218290447U (en) | 2023-01-13 |
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| CN202121241118.5U Active CN218290447U (en) | 2021-06-04 | 2021-06-04 | Waste sulfuric acid cracking regeneration system |
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2021
- 2021-06-04 CN CN202121241118.5U patent/CN218290447U/en active Active
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