CN215138333U - Production system for preparing liquid sulfur dioxide from sulfur dioxide enriched gas - Google Patents
Production system for preparing liquid sulfur dioxide from sulfur dioxide enriched gas Download PDFInfo
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- CN215138333U CN215138333U CN202121241551.9U CN202121241551U CN215138333U CN 215138333 U CN215138333 U CN 215138333U CN 202121241551 U CN202121241551 U CN 202121241551U CN 215138333 U CN215138333 U CN 215138333U
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Abstract
The utility model relates to a desulfurization flue gas handles technical field, concretely relates to sulfur dioxide enrichment gas system liquid sulfur dioxide's production system, including the multistage washing purifier, absorption tower, lean and rich liquid heat exchanger, desorber, vapour and liquid separator, multistage drying device, liquefying plant and the liquid sulfur dioxide storage tank that connect gradually. The production system can recycle the sulfur dioxide resource in the desulfurization and denitrification flue gas to avoid the secondary pollution of the sulfur dioxide in the flue gas to the environment, and simultaneously, the utilization rate of the sulfur resource is improved.
Description
Technical Field
The utility model relates to a desulfurization flue gas handles technical field, especially relates to a sulfur dioxide enrichment gas system liquid sulfur dioxide's production system.
Background
The power generation of a thermal power plant produces a large amount of sulfur and nitrate-containing waste gas in the burning coal, and the waste gas is discharged into the atmosphere to produce pollution and form acid rain. The desulfurization and denitrification system of the thermal power plant is a device for treating the waste gas containing a large amount of sulfur and nitrate. Sulfur dioxide (sulfur dioxide) is a colorless, non-flammable, pungent, and noxious gas that is discharged directly without treatment, causing serious environmental damage.
Tail gas discharged in industrial processes such as coal-fired power generation, mineral smelting and the like is a main source of sulfur dioxide pollutants in the atmosphere, the process for desulfurizing combustion tail gas is mature at present, and the subsequent resource utilization work of absorption products obtained by various desulfurization methods is still less. The sulfur dioxide has important application in the traditional sulfur chemical industry, and is generally used for producing sulfuric acid, liquid sulfur dioxide, high-purity sulfur, metal sulfite and other bulk sulfur chemical products, so that the method has important significance on recycling the sulfur dioxide in the sulfur-containing flue gas.
SUMMERY OF THE UTILITY MODEL
In order to solve the technical problem, an object of the utility model is to provide a sulfur dioxide enrichment gas system liquid sulfur dioxide's production system, production system can carry out recycle to the sulfur dioxide resource in the SOx/NOx control flue gas to avoid the sulfur dioxide in the flue gas to produce secondary pollution to the environment, simultaneously, improve the utilization ratio of sulfur resource.
In order to achieve the technical effects, the utility model adopts the following technical scheme:
the utility model provides a sulfur dioxide enrichment gas system liquid sulfur dioxide's production system, includes multistage washing purifier, absorption tower, poor rich liquid heat exchanger, desorber, vapour and liquid separator, multistage drying device, liquefying plant and the liquid sulfur dioxide storage tank that connects gradually, wherein:
a first liquid distributor, a filler and a first liquid storage tank are sequentially arranged in the absorption tower from top to bottom, and the multistage washing and purifying device is communicated with the first liquid storage tank through a first conveying pipeline;
the desorption tower is sequentially provided with a second liquid distributor, a first packing layer, a third liquid distributor, a second packing layer and a second liquid storage tank from top to bottom;
the lean-rich liquid heat exchanger is communicated with the first liquid storage tank through a second conveying pipeline, the lean-rich liquid heat exchanger is communicated with the desorption tower through a third conveying pipeline, and the discharge end of the third conveying pipeline is arranged between the first packing layer and the third liquid distributor;
the gas-liquid separator is communicated with the desorption tower through a fourth conveying pipeline, and the blanking end of the fourth conveying pipeline is arranged above the second liquid distributor.
Further, the lean-rich liquid heat exchanger is communicated with the absorption tower through a sixth conveying pipeline, the discharge end of the sixth conveying pipeline is arranged above the first liquid distributor, and a lean liquid recooler is further arranged on the sixth conveying pipeline.
Further, the desorption tower is further connected with a reboiler, a feeding pipeline is arranged on the reboiler, a baffle is arranged above the second liquid storage tank, the gas inlet end of the feeding pipeline is arranged on the baffle, and the reboiler is communicated with the second storage tank through a fifth conveying pipeline.
Further, a primary steam pipeline and a condensed water pipeline are further arranged on the reboiler.
Further, multistage washing purifier is including the one-level dynamic wave scrubber, filler scrubbing tower, second grade dynamic wave scrubber and one-level defroster and the second grade defroster that communicate in proper order, first pipeline's feed end with the second grade defroster intercommunication.
Further, the multistage drying device comprises a primary drying tower and a secondary drying tower.
Further, the liquefying device comprises a sulfur dioxide heat regenerator, a sulfur dioxide liquefier and a sulfur dioxide transfer tank which are sequentially connected, the sulfur dioxide heat regenerator is connected with the multistage drying device, the sulfur dioxide transfer tank is communicated with the sulfur dioxide heat regenerator through a seventh conveying pipeline, a transfer pump is arranged on the seventh conveying pipeline, and the sulfur dioxide heat regenerator is communicated with the liquid sulfur dioxide storage tank through an eighth conveying pipeline.
Compared with the prior art, the beneficial effects of the utility model are that: the utility model provides a pair of sulfur dioxide enrichment gas system liquid sulfur dioxide's production system at first carries out preliminary treatment to the sulfur dioxide flue gas through multistage washing purifier and purifies, rethread organic amine absorption tower absorbs sulfur dioxide in order to form the pregnant solution, and carry out the desorption to the pregnant solution through setting up the desorber, thereby isolate sulfur dioxide wherein, again through carrying out the drying to sulfur dioxide gas, the liquefaction, finally realize liquid sulfur dioxide's preparation, the recycle of the sulphur resource in the SOx/NOx control flue gas has been improved, and recovery efficiency is high, the liquid sulfur dioxide purity that makes is better.
Drawings
Fig. 1 is a schematic view of an overall structure of a production system for producing liquid sulfur dioxide from a sulfur dioxide-enriched gas according to an embodiment of the present invention;
fig. 2 is a schematic view of a partial enlarged structure at a position a of a production system for producing liquid sulfur dioxide from a sulfur dioxide-enriched gas according to an embodiment of the present invention;
the reference signs are: 11, a primary dynamic wave scrubber, 12, a packed wash column, 13, a secondary dynamic wave scrubber, 14, a primary demister, 15, a secondary demister, 151, a first transfer line, 20, an absorption column, 21, a first liquid distributor, 22, a packer, 23, a first reservoir, 30, a lean-rich liquid heat exchanger, 31, a second transfer line, 32, a third transfer line, 33, a sixth transfer line, 331, a lean liquid recooler, 40, a desorption column, 41, a tower top cooler, 42, a second liquid distributor, 43, a first packing layer, 44, a third liquid distributor, 45, a second packing layer, 46, a second reservoir, 47, a baffle, 50, a gas-liquid separator, 51, a fourth transfer line, 60, a reboiler, 61, a feed line, 62, a fifth transfer line, 63, a primary steam line, 64, a condensed water line, 71, a primary drying column, 72, a secondary drying tower 81, a sulfur dioxide regenerator 82, a sulfur dioxide liquefier 83, a sulfur dioxide transfer tank 84 and a liquid sulfur dioxide storage tank.
Detailed Description
Embodiments of the present invention will be described in detail below 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. 1-2, the system for producing liquid sulfur dioxide from a sulfur dioxide-enriched gas according to this embodiment includes a multi-stage washing and purifying device, an absorption tower 20, a lean and rich liquid heat exchanger 30, a desorption tower 40, a gas-liquid separator 50, a multi-stage drying device, a liquefaction device, and a liquid sulfur dioxide storage tank 84, which are connected in sequence.
In this embodiment, the multistage washing and purifying device includes a first dynamic wave scrubber 11, a packing washing tower 12, a second dynamic wave scrubber 13, a first demister 14 and a second demister 15, which are sequentially connected, and the second demister 15 is connected to the absorption tower 20 through a first conveying pipe 151. During specific implementation, sulfur dioxide enriched gas at the outlet of the existing desulfurization and denitrification system is firstly washed and purified by the primary dynamic wave washer 11, the filler washing tower 12, the secondary dynamic wave washer 13, the primary demister 14 and the secondary demister 15, the flue gas is cooled, dust and harmful components in the flue gas are removed, and the standard sulfur dioxide flue gas enters the absorption tower 20.
In this embodiment, a first liquid distributor 21, a filler 22 and a first liquid storage tank 23 are sequentially arranged in the absorption tower 20 from top to bottom, a discharge end of the first conveying pipeline 151 is arranged in the first liquid storage tank 23, and meanwhile, a barren solution pump is further arranged on the absorption tower 20 and used for pumping the organic amine absorbent in the first liquid storage tank 23 to a position above the first liquid distributor 21. The desorption tower 40 is internally provided with a tower top cooler 41, a second liquid distributor 42, a first filler layer 43, a third liquid distributor 44, a second filler layer 45 and a second liquid storage tank 46 from top to bottom in sequence. The lean-rich liquid heat exchanger 30 is arranged between the absorption tower 20 and the desorption tower 40, the lean-rich liquid heat exchanger 30 is communicated with the first liquid storage tank 23 through a second conveying pipeline 31, the lean-rich liquid heat exchanger 30 is communicated with the desorption tower 40 through a third conveying pipeline 32, and the discharge end of the third conveying pipeline 32 is arranged between the first packing layer 43 and the third liquid distributor 44. Meanwhile, the lean-rich liquid heat exchanger 30 is communicated with the absorption tower 20 through a sixth conveying pipeline 33, a discharge end of the sixth conveying pipeline 33 is arranged above the first liquid distributor 21, and a lean liquid recooler 331 is further arranged on the sixth conveying pipeline 33. The gas-liquid separator 50 is communicated with the desorption tower 40 through a fourth conveying pipeline 51, and a blanking end of the fourth conveying pipeline 51 is arranged above the tower top cooler 41. More specifically, the first liquid storage tank 23 stores therein an organic amine absorbent, which is a regenerable sulfur dioxide gas absorbent, the organic amine absorbent after absorbing the sulfur dioxide gas becomes a rich liquid, and the rich liquid is called a lean liquid after resolving the sulfur dioxide gas in the desorption tower 40. In specific implementation, the purified and washed sulfur dioxide flue gas enters the absorption tower 20 from the lower part of the absorption tower 20, the barren solution is pumped to the upper part of the first liquid distributor 21 from the first liquid storage tank 23 by the barren solution pump, the barren solution uniformly falls along the filler 22 under the distribution of the first liquid distributor 21, the barren solution is fully contacted with the sulfur dioxide flue gas flowing upwards from the lower part of the tower in the filler 22, the barren solution fully absorbs sulfur dioxide in the flue gas, and the flue gas after the sulfur dioxide gas is absorbed is discharged after reaching the standard or is sent back to the desulfurization and denitrification system. And the barren solution in the first liquid storage tank 23 is changed into rich solution after absorbing sulfur dioxide and is conveyed to the barren and rich solution heat exchanger 30 from the first liquid storage tank 23, the rich solution enters the third liquid distributor 44 at the upper part of the second packing layer 45 from the middle part of the desorption tower 40 after passing through the barren and rich solution heat exchanger, and uniformly falls along the second packing layer 45 to be contacted with the water vapor rising from the bottom of the desorption tower 40, due to the heating action, the sulfur dioxide contained in the rich solution is released, and rises together with the water vapor, and passes through the tower top cooler 41, under the indirect cooling action of cooling water, most of the water vapor is condensed into water, and the rest of the water vapor continues to enter the gas-liquid separator 50.
In this embodiment, a reboiler 60 is further connected to the desorption tower 40, a feed pipe 61 is provided on the reboiler 60, a baffle 47 is provided above the second reservoir 46, and a gas inlet end of the feed pipe 61 is provided above the baffle 47, and the reboiler 60 is communicated with the second reservoir through a fifth transfer pipe 62. Meanwhile, a primary steam pipeline 63 and a condensed water pipeline 64 are further arranged on the reboiler 60, the primary steam pipeline 63 is used for conveying low-pressure primary steam, and the condensed water pipeline 64 is used for discharging condensed water. In a specific embodiment, in order to avoid the absorption liquid in the desorption tower from being mixed with steam and causing the composition of the absorption liquid to change, the low-pressure primary steam for heating is not directly contacted with the absorption liquid, but indirectly heats the lean liquid falling to the bottom of the tower through the reboiler 60, so that the water in the absorption liquid is evaporated into steam, and the steam is used to contact with the rich liquid in the packed tower to release the sulfur dioxide contained in the rich liquid. After the low-pressure primary steam is contacted with the lean solution in the reboiler 60 for heat exchange, the steam is condensed into water, and the condensed water is sent out of a boundary area through the condensed water pipeline 64 for other workshops to use. And the high-temperature barren solution at the bottom of the desorption tower 40 is sent into a barren and rich solution heat exchanger through a barren solution pump to indirectly exchange heat with the rich solution to recover heat, and then is further cooled by a barren solution recooler 331 to become barren solution which can be used for absorbing sulfur dioxide gas again, and is sent into the absorption tower 20 to circularly absorb the sulfur dioxide gas in the flue gas.
In this embodiment, the multistage drying apparatus includes a primary drying tower 71 and a secondary drying tower 72. The liquefying device comprises a sulfur dioxide heat regenerator 81, a sulfur dioxide liquefier 82 and a sulfur dioxide transfer tank 83 which are sequentially connected, wherein the sulfur dioxide heat regenerator 81 is connected with the multistage drying device, the sulfur dioxide transfer tank 83 is communicated with the sulfur dioxide heat regenerator 81 through a seventh conveying pipeline, a transfer pump is arranged on the seventh conveying pipeline, and the sulfur dioxide heat regenerator 81 is communicated with the liquid sulfur dioxide storage tank 84 through an eighth conveying pipeline. In specific implementation, the gas-water mixture at the outlet of the cooler 41 at the top of the desorption tower 40 continuously enters the gas-liquid separator 50 for gas-water separation, and the separated water is pumped back to the second liquid distributor 42 above the first packing layer 43 of the desorption tower 40 and returns to the absorption liquid system. And the sulfur dioxide gas separated from most of liquid water is sent to a sulfur dioxide regenerator 81 for cooling after sequentially passing through a primary drying tower 71 and a secondary drying tower 72 for secondary drying, and then sent to a sulfur dioxide liquefier 82 for freezing and liquefying after cooling, the liquefied liquid sulfur dioxide enters a liquid sulfur dioxide transfer tank 83, is pressurized by a liquid sulfur dioxide transfer pump and sent to the sulfur dioxide regenerator 81 for heat exchange with the sulfur dioxide gas from the secondary drying tower 72, and finally is sent to a liquid sulfur dioxide storage tank 84 for storage.
Although the present invention has been described in detail with reference to the preferred embodiments, those skilled in the art will understand that the present invention can be modified or replaced with other embodiments without departing from the spirit and scope of the present invention, which should be construed as limited only by the appended claims. The technology, shape and construction parts which are not described in detail in the present invention are all known technology.
Claims (7)
1. The utility model provides a sulfur dioxide enrichment gas system liquid sulfur dioxide's production system which characterized in that, includes multistage washing purifier, absorption tower (20), poor rich liquid heat exchanger (30), desorber (40), vapour and liquid separator (50), multistage drying device, liquefaction device and liquid sulfur dioxide storage tank (84) that connect gradually, wherein:
a first liquid distributor (21), a filler (22) and a first liquid storage tank (23) are sequentially arranged in the absorption tower (20) from top to bottom, and the multistage washing and purifying device is communicated with the first liquid storage tank (23) through a first conveying pipeline (151);
the desorption tower (40) is sequentially provided with a second liquid distributor (42), a first filler layer (43), a third liquid distributor (44), a second filler layer (45) and a second liquid storage tank (46) from top to bottom;
the lean-rich liquid heat exchanger (30) is communicated with the first liquid storage tank (23) through a second conveying pipeline (31), the lean-rich liquid heat exchanger (30) is communicated with the desorption tower (40) through a third conveying pipeline (32), and the discharge end of the third conveying pipeline (32) is arranged between the first packing layer (43) and the third liquid distributor (44);
the gas-liquid separator (50) is communicated with the desorption tower (40) through a fourth conveying pipeline (51), and the blanking end of the fourth conveying pipeline (51) is arranged above the second liquid distributor (42).
2. The system for producing liquid sulfur dioxide from a sulfur dioxide-enriched gas as claimed in claim 1, wherein: the lean-rich liquid heat exchanger (30) is communicated with the absorption tower (20) through a sixth conveying pipeline (33), the discharge end of the sixth conveying pipeline (33) is arranged above the first liquid distributor (21), and a lean liquid recooler (331) is further arranged on the sixth conveying pipeline (33).
3. The system for producing liquid sulfur dioxide from a sulfur dioxide-enriched gas as claimed in claim 1, wherein: the desorption tower (40) is further connected with a reboiler (60), a feeding pipeline (61) is arranged on the reboiler (60), a baffle (47) is arranged above the second liquid storage tank (46), the gas inlet end of the feeding pipeline (61) is arranged on the baffle (47), and the reboiler (60) is communicated with the second storage tank through a fifth conveying pipeline (62).
4. The system for producing liquid sulfur dioxide from a sulfur dioxide-enriched gas as claimed in claim 3, wherein: the reboiler (60) is also provided with a primary steam pipeline (63) and a condensed water pipeline (64).
5. The system for producing liquid sulfur dioxide from a sulfur dioxide-enriched gas as claimed in claim 1, wherein: the multistage washing and purifying device comprises a first-stage dynamic wave washer (11), a filler washing tower (12), a second-stage dynamic wave washer (13), a first-stage demister (14) and a second-stage demister (15), wherein the first-stage dynamic wave washer, the second-stage dynamic wave washer and the second-stage demister are sequentially communicated, and the feeding end of a first conveying pipeline (151) is communicated with the second-stage demister (15).
6. The system for producing liquid sulfur dioxide from a sulfur dioxide-enriched gas as claimed in claim 1, wherein: the multistage drying device comprises a primary drying tower (71) and a secondary drying tower (72).
7. The system for producing liquid sulfur dioxide from a sulfur dioxide-enriched gas as claimed in claim 1, wherein: the liquefying device comprises a sulfur dioxide heat regenerator (81), a sulfur dioxide liquefier (82) and a sulfur dioxide transfer tank (83) which are sequentially connected, wherein the sulfur dioxide heat regenerator (81) is connected with a multistage drying device, the sulfur dioxide transfer tank (83) is communicated with the sulfur dioxide heat regenerator (81) through a seventh conveying pipeline, a transfer pump is arranged on the seventh conveying pipeline, and the sulfur dioxide heat regenerator (81) is communicated with a liquid sulfur dioxide storage tank (84) through an eighth conveying pipeline.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121241551.9U CN215138333U (en) | 2021-06-04 | 2021-06-04 | Production system for preparing liquid sulfur dioxide from sulfur dioxide enriched gas |
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| CN202121241551.9U CN215138333U (en) | 2021-06-04 | 2021-06-04 | Production system for preparing liquid sulfur dioxide from sulfur dioxide enriched gas |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114887467A (en) * | 2022-05-26 | 2022-08-12 | 苏州璞赛环境科技有限公司 | Gas-phase sulfur dioxide tail gas treatment system and treatment method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114887467A (en) * | 2022-05-26 | 2022-08-12 | 苏州璞赛环境科技有限公司 | Gas-phase sulfur dioxide tail gas treatment system and treatment method |
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