CN111495118A - Moving bed type low-temperature flue gas adsorption desulfurization device - Google Patents
Moving bed type low-temperature flue gas adsorption desulfurization device Download PDFInfo
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- CN111495118A CN111495118A CN202010420534.5A CN202010420534A CN111495118A CN 111495118 A CN111495118 A CN 111495118A CN 202010420534 A CN202010420534 A CN 202010420534A CN 111495118 A CN111495118 A CN 111495118A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
- B01D53/08—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds according to the "moving bed" method
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
Abstract
The invention discloses a moving bed type low-temperature flue gas adsorption desulfurization device, which comprises a dedusted flue gas input pipeline, a desulfurized flue gas pipeline, a booster fan, a flue gas waste heat recoverer, a flue gas cooling system, a moving bed adsorption tower and a desorption tower, wherein the dedusted flue gas input pipeline is connected with the booster fan; the flue gas input pipeline after dust removal is communicated with the inlet of a flue gas waste heat recoverer through a booster fan, the outlet of the flue gas waste heat recoverer is communicated with the inlet of a flue gas cooling system, the outlet of the flue gas cooling system is communicated with the flue gas inlet of a moving bed adsorption tower, the porous adsorbent outlet at the bottom of the moving bed adsorption tower is communicated with the inlet of a desorption tower, the porous adsorbent outlet of the desorption tower is communicated with the porous adsorbent inlet at the top of the moving bed adsorption tower, the gas outlet of the moving bed adsorption tower is communicated with the flue gas pipeline after sulfur removal, and the device is used for2The adsorption capacity is large, the adsorption equipment is small, the loss of the adsorbent is low, and the safety is high.
Description
Technical Field
The invention belongs to the technical field of flue gas desulfurization, and relates to a moving bed type low-temperature flue gas adsorption desulfurization device.
Background
The flue gas generated by burning coal contains a large amount of SO2It is one of the main causes of air pollution. At present, the mainstream desulfurization technology of coal-fired flue gas is limestone-gypsum wet desulfurization technology, and SO is subjected to wet desulfurization2And reacting with limestone slurry to generate insoluble calcium sulfate (gypsum) for removal. The wet desulphurization uses a large amount of limestone as a desulfurizer, the serious mountain destruction is caused by the large amount of exploitation of the limestone, and the treatment problem of a power plant is also brought by the generation of a large amount of desulphurization wastewater.
In addition, the dry active coke (charcoal) desulfurization technology is one of the mature desulfurization technologies at present, and is widely applied in japan, germany and our country. The operation temperature of the active coke (carbon) dry desulfurization technology is generally 100-150 ℃ for adsorption, and the SO is absorbed at the temperature2With H in the flue gas2O and O2Reaction to form H2SO4Thus SO2By chemisorption with H2SO4The form of (2) realizes adsorption. Adsorbed H2SO4Heating for regeneration to generate high-concentration SO2To prepare products such as sulfuric acid or sulfur; or by washing with water and regenerating2SO4And (6) washing to obtain the finished product.
The adsorption and heating regeneration mechanism of the dry desulfurization of the activated coke (carbon) is as follows:
and (3) adsorption reaction: SO (SO)2+H2O+1/2O2＝H2SO4
Heating and regenerating reaction: 2H2SO4+C→CO2+2SO2+2H2O (350-450 ℃ main reaction)
H2SO4+C→CO+SO2+H2O (main reaction at 450 ℃ C. or higher)
The dry active coke (charcoal) desulfurization technique has the following disadvantages:
1. sulfur capacity (SO)2Adsorption capacity) is low, generally lower than 30mg/g, activityThe coke (carbon) loading amount is large, and the adsorption equipment is large;
2. the heating regeneration temperature is high, generally higher than 350 ℃, the heat consumption is large, and the spontaneous combustion of the active coke (carbon) is easy to generate, so the contact with oxygen is prevented in the regeneration process, and the safety is poor;
3. in the heating regeneration process, active coke (carbon) participates in the reaction, the consumption of the adsorbent is large, and the regenerated gas contains a large amount of CO2CO, etc., affecting SO2And (4) recycling.
The conventional active coke (charcoal) dry desulfurization device is shown as a figure 1.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a moving bed type low-temperature flue gas adsorption desulfurization device which is used for SO2The adsorption capacity is large, the adsorption equipment is small, the loss of the adsorbent is low, and the safety is high.
In order to achieve the aim, the moving bed type low-temperature flue gas adsorption desulfurization device comprises a flue gas input pipeline after dust removal, a booster fan, a flue gas waste heat recoverer, a flue gas cooling system, a flue gas pipeline after sulfur removal, a moving bed adsorption tower and a desorption tower;
the flue gas input pipeline after dust removal is communicated with the inlet of the flue gas waste heat recoverer through a booster fan, the outlet of the flue gas waste heat recoverer is communicated with the inlet of a flue gas cooling system, the outlet of the flue gas cooling system is communicated with the flue gas inlet of a moving bed adsorption tower, the porous adsorbent outlet at the bottom of the moving bed adsorption tower is communicated with the inlet of a desorption tower, the porous adsorbent outlet of the desorption tower is communicated with the porous adsorbent inlet at the top of the moving bed adsorption tower, and the gas outlet of the moving bed adsorption tower is communicated with the flue gas pipeline after sulfur removal.
The flue gas cooling system adopts a two-section type spray cooling structure.
The flue gas cooling system adopts a three-section type spray cooling structure.
The porous adsorbent outlet of the desorption tower is communicated with the porous adsorbent inlet at the top of the moving bed adsorption tower through a chain bucket lifting device.
The porous adsorbent is active coke or molecular sieve.
When the flue gas cooling system works, the dedusted high-temperature flue gas is sent into a flue gas waste heat recoverer through a booster fan, the temperature of the flue gas is reduced to be below 70 ℃ through the flue gas waste heat recoverer, wherein the recovered heat is used for supplying hot water and steam or for refrigeration, the flue gas after waste heat recovery enters a flue gas cooling system, the flue gas is cooled to a temperature region below room temperature through a spraying cooling or indirect heat exchange mode, wherein the temperature region above the room temperature is cooled and the heat is taken away through cooling water, and the temperature region below the room temperature is cooled in a refrigeration mode; the cooled flue gas enters a moving bed adsorption tower, contacts with a porous adsorbent filled in the moving bed adsorption tower, and removes SO in the flue gas in a physical adsorption mode2Then the sulfur-containing gas enters a flue gas pipeline after sulfur is removed, the porous adsorbent saturated in adsorption is discharged from the bottom of a moving bed adsorption tower in a self-weight blanking mode, the gas enters a desorption tower, the porous adsorbent saturated in adsorption is regenerated in the desorption tower in a heating or vacuumizing mode, and SO is desorbed2A gas; and feeding the desorbed porous adsorbent to the top of a moving bed adsorption tower for reuse.
The invention has the following beneficial effects:
when the moving bed type low-temperature flue gas adsorption desulfurization device is in specific operation, the flue gas is cooled through the flue gas waste heat recoverer and the flue gas cooling system, SO that SO is treated2In addition, the invention adopts a physical adsorption mode, is easy to desorb, has low desorption temperature, low heat consumption, difficult spontaneous combustion of the adsorbent and higher safety, can desorb by adopting a vacuum suction mode, simultaneously, the adsorbent does not participate in the reaction in the desorption process, the adsorbent hardly generates loss, and can continuously run under the condition of no adsorbent supplement. In addition, a large amount of acidic condensate water separated out in the flue gas cooling process can be supplied to a power plant after neutralization treatment, so that the water consumption of the power plant is reduced, and the method can be widely applied to flue gas desulfurization of flue gas of the power plant, sintering flue gas of a steel mill, coke oven flue gas and the like.
Drawings
FIG. 1 is a schematic diagram of a prior art structure;
fig. 2 is a schematic structural diagram of the present invention.
Wherein, 1 is a booster fan, 2 is a flue gas waste heat recoverer, 3 is a flue gas cooling system, 4 is a moving bed adsorption tower, and 5 is a desorption tower.
Detailed Description
The invention is described in further detail below with reference to the accompanying drawings:
referring to fig. 2, the moving bed type low-temperature flue gas adsorption desulfurization device of the present invention includes a flue gas input pipeline after dust removal, a booster fan 1, a flue gas waste heat recoverer 2, a flue gas cooling system 3, a moving bed adsorption tower 4, a desorption tower 5, and a flue gas pipeline after sulfur removal; the flue gas input pipeline after dust removal is communicated with the inlet of a flue gas waste heat recoverer 2 through a booster fan 1, the outlet of the flue gas waste heat recoverer 2 is communicated with the inlet of a flue gas cooling system 3, the outlet of the flue gas cooling system 3 is communicated with the flue gas inlet of a moving bed adsorption tower 4, the porous adsorbent outlet at the bottom of the moving bed adsorption tower 4 is communicated with the inlet of a desorption tower 5, the porous adsorbent outlet of the desorption tower 5 is communicated with the porous adsorbent inlet at the top of the moving bed adsorption tower 4, and the gas outlet of the moving bed adsorption tower 4 is communicated with the flue gas pipeline after sulfur removal.
A porous adsorbent outlet of the desorption tower 5 is communicated with a porous adsorbent inlet at the top of the moving bed adsorption tower 4 through a chain bucket lifting device; the porous adsorbent is active coke or molecular sieve.
When the flue gas cooling system works, the dedusted high-temperature flue gas is sent into a flue gas waste heat recoverer 2 through a booster fan 1, the temperature of the flue gas is reduced to be below 70 ℃ through the flue gas waste heat recoverer 2, the recovered heat is used for supplying hot water and steam or for refrigeration, the flue gas after waste heat recovery enters a flue gas cooling system 3, and is cooled to a temperature region below room temperature through a spraying cooling or indirect heat exchange mode, wherein the temperature region above the room temperature is cooled and the heat is taken away through cooling water, and the temperature region below the room temperature is cooled in a refrigeration mode; the cooled flue gas enters a moving bed adsorption tower 4, contacts with a porous adsorbent filled in the moving bed adsorption tower 4 and passes through a physical adsorption methodFormula SO in desorption flue gas2Then the sulfur-containing gas enters a flue gas pipeline after sulfur is removed, the porous adsorbent saturated in adsorption is discharged from the bottom of a moving bed adsorption tower 4 in a self-weight blanking mode, the gas enters a desorption tower 5, the porous adsorbent saturated in adsorption is regenerated in the desorption tower 5 in a heating or vacuumizing mode, and SO is desorbed2A gas; and (4) feeding the desorbed porous adsorbent to the top of the moving bed adsorption tower 4 for reuse.
Example one
Flue gas of 600MW coal-fired unit (flue gas flow 200 ten thousand standard square/hour, SO)2Content 3000mg/Nm3) After denitration and dust removal, the flue gas enters the invention, after being pressurized by a booster fan 1, the flue gas enters a flue gas waste heat recoverer 2, the temperature of the flue gas is reduced from 120 ℃ to 70 ℃, and meanwhile, hot water of 80-90 ℃ is generated and enters a heat supply pipe network; the flue gas with the temperature of 70 ℃ enters a flue gas cooling system 3 and is cooled to 5 ℃ in a spray cooling mode, the flue gas cooling system 3 adopts a two-section spray cooling mode, the temperature of the first section is reduced to 35 ℃ by spraying, the temperature of the second section is reduced to 5 ℃ by spraying chilled water, the first section of spray circulation liquid is cooled by cooling water, and the second section of spray circulation liquid is cooled by a water chiller; the low-temperature flue gas cooled to 5 ℃ by the flue gas cooling system 3 enters the moving bed adsorption tower 4, the moving bed adsorption tower 4 adopts a cross flow mode, the flue gas horizontally passes through the adsorption bed layers, and the active coke adsorbent vertically flows through the moving bed adsorption tower 4 from top to bottom. SO in the flue gas after the flue gas flows through the moving bed adsorption tower 42Is adsorbed by the active coke, and the purified flue gas is discharged from the moving bed adsorption tower 4. The active coke with saturated adsorption is discharged from the bottom of the moving bed adsorption tower 4 and enters a desorption tower 5 in a self-weight blanking mode, the desorption tower 5 is divided into an upper section and a lower section, the upper section is a heating desorption section, and the active coke with saturated adsorption is desorbed to remove high-concentration SO under the blowing of hot air at 150 DEG C2And the lower section of the desorption gas is a cooling section, the temperature of the active coke is reduced to room temperature through cold air purging, the regenerated active coke desorbed by the desorption tower 5 is discharged from the bottom of the desorption tower 5, and is lifted to the top of the moving bed adsorption tower 4 through a bucket elevator to be fed, so that closed circulation is formed and continuous operation is realized.
Whole moving bedIn the circulation process, the feeding and discharging rates of the moving bed adsorption tower 4 and the desorption tower 5 are kept consistent, and the flow rate of the active coke is controlled by a star-shaped discharger at the bottom of the desorption tower 5. Residual SO in the clean flue gas discharged from the moving bed adsorption tower 42The concentration is adjusted by adjusting the flow rate of the active coke, when the concentration exceeds the standard, the flow rate of the active coke needs to be improved, when the adsorption desulfurization is carried out at 5 ℃, the saturated sulfur capacity is about 80mg/g, the loading amount of the active coke in the adsorption tower 4 of the moving bed is 300 tons, and the circulation amount of the active coke is 75 tons/h.
Example two
The second embodiment is consistent with the first embodiment in the whole operation process, and the difference is that the flue gas cooling system 3 adopts a three-section spray cooling mode, the flue gas with the temperature of 70 ℃ after waste heat recovery is cooled to-20 ℃, the first section is cooled to 35 ℃ by spraying, the second section is cooled to 5 ℃ by spraying chilled water, the third section is cooled to-20 ℃ by spraying low-temperature calcium chloride solution, the first section is cooled by cooling water, and the second section is cooled by a water chiller; the third section of spray circulation liquid (calcium chloride solution) is cooled by a low-temperature refrigerating unit. The flue gas cooled to-20 ℃ enters a moving bed adsorption tower 4 for low-temperature SO2And (4) adsorbing. The active coke desorption regeneration process is consistent with the embodiment, the active coke discharging and feeding circulation is consistent with the embodiment, and the second embodiment is different from the first embodiment in that the adsorption temperature is lower, the adsorption capacity is larger, so the active coke loading and circulation capacity are smaller, the tower equipment is smaller, but the energy consumption for cooling flue gas is larger, the saturated sulfur capacity is about 170mg/g when adsorption desulfurization is carried out at-20 ℃, the active coke loading of the moving bed adsorption tower 4 is 150 tons, and the active coke circulation capacity is 35 tons/hour.
Claims (4)
1. A moving bed type low-temperature flue gas adsorption desulfurization device is characterized by comprising a flue gas input pipeline after dust removal, a booster fan (1), a flue gas waste heat recoverer (2), a flue gas cooling system (3), a moving bed adsorption tower (4), a desorption tower (5) and a flue gas pipeline after desulfurization;
the dedusted flue gas input pipeline is communicated with an inlet of a flue gas waste heat recoverer (2) through a booster fan (1), an outlet of the flue gas waste heat recoverer (2) is communicated with an inlet of a flue gas cooling system (3), an outlet of the flue gas cooling system (3) is communicated with a flue gas inlet of a moving bed adsorption tower (4), a porous adsorbent outlet at the bottom of the moving bed adsorption tower (4) is communicated with an inlet of a desorption tower (5), a porous adsorbent outlet of the desorption tower (5) is communicated with a porous adsorbent inlet at the top of the moving bed adsorption tower (4), and a gas outlet of the moving bed adsorption tower (4) is communicated with a flue gas pipeline after sulfur removal;
the flue gas cooling system (3) adopts a two-section type spray cooling structure or a three-section type spray cooling structure.
2. The moving bed type flue gas low-temperature adsorption desulfurization device according to claim 1, characterized in that the porous adsorbent outlet of the desorption tower (5) is communicated with the porous adsorbent inlet at the top of the moving bed adsorption tower (4) through a bucket chain lifting device.
3. The moving bed type low temperature flue gas adsorption desulfurization device of claim 1, wherein the porous adsorbent is activated coke or molecular sieve.
4. The moving bed type low-temperature flue gas adsorption desulfurization device of claim 1, wherein, in operation, the dedusted high-temperature flue gas is sent into a flue gas waste heat recoverer (2) through a booster fan (1), the flue gas temperature is reduced to below 70 ℃ through the flue gas waste heat recoverer (2), wherein the recovered heat is used for supplying hot water, steam or refrigerating, the flue gas subjected to waste heat recovery enters a flue gas cooling system (3), and is cooled to a temperature zone below room temperature through a spray cooling or indirect heat exchange mode, wherein the temperature zone above the room temperature takes away the heat through cooling water, and the temperature zone below the room temperature is cooled by adopting a refrigerating mode; the cooled flue gas enters a moving bed adsorption tower (4), contacts with a porous adsorbent filled in the moving bed adsorption tower (4), and removes SO in the flue gas in a physical adsorption mode2Then the sulfur-containing porous adsorbent enters a sulfur-containing flue gas pipeline to be communicated, the porous adsorbent saturated in adsorption is discharged from the bottom of a moving bed adsorption tower (4) in a self-weight blanking mode, enters a desorption tower (5) and is desorbedIn the absorption tower (5), the porous adsorbent saturated in absorption is regenerated by heating or vacuumizing, and SO is desorbed2A gas; and the porous adsorbent after desorption is sent to the top of the moving bed adsorption tower (4) for repeated use.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111841066A (en) * | 2020-08-14 | 2020-10-30 | 中国华能集团清洁能源技术研究院有限公司 | System and method for removing acid gas in flue gas |
| WO2021232692A1 (en) * | 2020-05-18 | 2021-11-25 | 中国华能集团有限公司 | Method for low temperature adsorption and desulfurization of flue gas |
| WO2021232693A1 (en) * | 2020-05-18 | 2021-11-25 | 中国华能集团有限公司 | Flue gas integrated desulfurization and denitration method based on low-temperature adsorption principle |
| WO2022032860A1 (en) * | 2020-08-14 | 2022-02-17 | 中国华能集团清洁能源技术研究院有限公司 | Near-zero emission-type flue gas multi-pollutant integrated removal system and method |
-
2020
- 2020-05-18 CN CN202010420534.5A patent/CN111495118A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2021232692A1 (en) * | 2020-05-18 | 2021-11-25 | 中国华能集团有限公司 | Method for low temperature adsorption and desulfurization of flue gas |
| WO2021232693A1 (en) * | 2020-05-18 | 2021-11-25 | 中国华能集团有限公司 | Flue gas integrated desulfurization and denitration method based on low-temperature adsorption principle |
| CN111841066A (en) * | 2020-08-14 | 2020-10-30 | 中国华能集团清洁能源技术研究院有限公司 | System and method for removing acid gas in flue gas |
| WO2022032860A1 (en) * | 2020-08-14 | 2022-02-17 | 中国华能集团清洁能源技术研究院有限公司 | Near-zero emission-type flue gas multi-pollutant integrated removal system and method |
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