CN111495113A - Fixed bed type low-temperature flue gas adsorption desulfurization system and method - Google Patents
Fixed bed type low-temperature flue gas adsorption desulfurization system and method Download PDFInfo
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- CN111495113A CN111495113A CN202010421605.3A CN202010421605A CN111495113A CN 111495113 A CN111495113 A CN 111495113A CN 202010421605 A CN202010421605 A CN 202010421605A CN 111495113 A CN111495113 A CN 111495113A
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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
- B01D53/04—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 stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
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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
- B01D53/04—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 stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0438—Cooling or heating systems
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
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Abstract
The invention discloses a fixed bed type flue gas low-temperature adsorption desulfurization system and a method, which comprises a flue gas input pipeline after dust removal, a flue gas induced draft fan, a flue gas waste heat recoverer, a cooling system, a flue gas switching device, a cold energy recoverer, a flue gas output pipeline and a plurality of fixed bed adsorption towers; the outlet of the flue gas input pipeline after dust removal is communicated with the inlet of a flue gas induced draft fan, the outlet of the flue gas induced draft fan is communicated with the inlet of a flue gas waste heat recoverer, the outlet of the flue gas waste heat recoverer is communicated with the inlet of a cooling system, the outlet of the cooling system is communicated with the inlet of a flue gas switching device, the outlet of the flue gas switching device is respectively communicated with the inlets of fixed bed adsorption towers, the outlet of each fixed bed adsorption tower is communicated with the inlet of a cold energy recoverer, and the outlet of the cold energy recoverer is communicated with a flue gas output pipeline2The adsorption capacity is large, the filling amount of the adsorbent is small, the adsorption equipment is small, the safety is high, and the consumption of the adsorbent is low.
Description
Technical Field
The invention belongs to the technical field of flue gas desulfurization, and relates to a fixed bed type flue gas low-temperature adsorption desulfurization system and method.
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)2The adsorption capacity) is lower, generally lower than 30mg/g, the loading capacity of the activated coke (carbon) 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 process is shown in the attached figure 1.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a fixed bed type low-temperature flue gas adsorption desulfurization system and a fixed bed type low-temperature flue gas adsorption desulfurization method, wherein SO is contained in the system and the method2The adsorption capacity is large, the filling amount of the adsorbent is small, the adsorption equipment is small, the safety is high, and the consumption of the adsorbent is low.
In order to achieve the aim, the fixed bed type low-temperature flue gas adsorption desulfurization system comprises a dedusted flue gas input pipeline, a flue gas induced draft fan, a flue gas waste heat recoverer, a cooling system, a flue gas switching device, a cold energy recoverer, a flue gas output pipeline and a plurality of fixed bed adsorption towers;
the outlet of the flue gas input pipeline after dust removal is communicated with the inlet of a flue gas induced draft fan, the outlet of the flue gas induced draft fan is communicated with the inlet of a flue gas waste heat recoverer, the outlet of the flue gas waste heat recoverer is communicated with the inlet of a cooling system, the outlet of the cooling system is communicated with the inlet of a flue gas switching device, the outlet of the flue gas switching device is respectively communicated with the inlets of the fixed bed adsorption towers, the outlet of each fixed bed adsorption tower is communicated with the inlet of a cold energy recoverer, and the outlet of the cold energy recoverer is communicated with a flue;
the cooling system is a two-section spray cooling structure or a three-section spray cooling structure.
The number of the fixed bed adsorption towers is two.
And a porous adsorption material is filled in the fixed bed adsorption tower, wherein the porous adsorption material is activated carbon, activated coke or a molecular sieve.
The fixed bed type low-temperature flue gas adsorption desulfurization method comprises the following steps:
the flue gas enters a flue gas induced draft fan through a flue gas input pipeline after dust removal, is pressurized by the flue gas induced draft fan and then is sent into a flue gas waste heat recoverer to be cooled to-20 ℃, then is sent into any fixed bed adsorption tower through a flue gas switching device, is subjected to desulfurization treatment through the fixed bed adsorption tower, the flue gas output by the fixed bed adsorption tower enters a cold energy recoverer to recover cold energy, and is finally discharged through a flue gas output pipeline, and the cold energy recovered by the cold energy recoverer is used for cooling the flue gas or cooling a refrigerant of a refrigerating system.
When SO is adsorbed2When the penetration begins, the adsorption saturation of the current fixed bed adsorption tower is indicated, the flue gas is input into any other fixed bed adsorption tower through the flue gas switching device, and the SO is carried out on the saturated fixed bed adsorption tower at the same time2Desorbing by heating or vacuum desorption to obtain SO2Gas for preparing liquid SO2Sulfuric acid, sulfur and sulfates.
The invention has the following beneficial effects:
during specific operation, the fixed bed type low-temperature flue gas adsorption desulfurization system and the method cool the flue gas through the cooling system and the flue gas waste heat recoverer, and then carry out SO in the flue gas through the fixed adsorption tower2Carrying out adsorption of SO2The adsorption temperature is low, the adsorption is carried out below room temperature, the adsorption capacity is large, the adsorbent filling amount is small, the adsorption equipment is small, the fixed bed mode is adopted for carrying out adsorption and desorption alternate operation, the abrasion loss of the adsorbent is avoided, the problems of blanking blockage and the like caused by a moving bed are avoided, in addition, the flue gas is adsorbed after being condensed and dehumidified, the moisture content is low, the physical adsorption is mainly used, and H is formed2SO4The method has the advantages of low chemical adsorption proportion, easiness in desorption of physical adsorption, low desorption temperature, low heat consumption, difficulty in spontaneous combustion of the adsorbent, high safety and easiness in desorption of physical adsorption, can be used for desorption in a vacuum suction mode, simultaneously the adsorbent does not participate in reaction in the desorption process, and the adsorbent hardly generates loss.
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 flue gas induced draft fan, 2 is a flue gas waste heat recoverer, 3 is a cooling system, 4 is a flue gas switching device, 5 is a fixed bed adsorption tower, and 6 is a cold energy recoverer.
Detailed Description
The invention is described in further detail below with reference to the accompanying drawings:
referring to fig. 2, the fixed bed type flue gas low temperature adsorption desulfurization system of the present invention includes a flue gas input pipeline after dust removal, a flue gas induced draft fan 1, a flue gas waste heat recoverer 2, a cooling system 3, a flue gas switching device 4, a cold energy recoverer 6, a flue gas output pipeline, and a plurality of fixed bed adsorption towers 5; the outlet of the flue gas input pipeline after dust removal is communicated with the inlet of a flue gas induced draft fan 1, the outlet of the flue gas induced draft fan 1 is communicated with the inlet of a flue gas waste heat recoverer 2, the outlet of the flue gas waste heat recoverer 2 is communicated with the inlet of a cooling system 3, the outlet of the cooling system 3 is communicated with the inlet of a flue gas switching device 4, the outlet of the flue gas switching device 4 is respectively communicated with the inlets of fixed bed adsorption towers 5, the outlet of each fixed bed adsorption tower 5 is communicated with the inlet of a cold energy recoverer 6, and the outlet of the cold energy recoverer 6 is communicated with a flue gas.
The number of the fixed bed adsorption towers 5 is two; and a porous adsorption material is filled in the fixed bed adsorption tower 5, wherein the porous adsorption material is activated carbon, activated coke or a molecular sieve.
The fixed bed type low-temperature flue gas adsorption desulfurization method comprises the following steps:
introducing the dedusted high-temperature flue gas into a flue gas waste heat recoverer 2 through a flue gas induced draft fan 1, and reducing the temperature of the flue gas to be below 70 ℃, wherein the recovered heat is used for supplying hot water and steam or for refrigeration; the flue gas after waste heat recovery enters a cooling system 3, and is cooled to a temperature area below room temperature by a spray cooling or indirect heat exchange mode, the temperature area above the room temperature is cooled, heat is taken away by cooling water, and the temperature area below the room temperature is cooled by a refrigeration mode; the cooled flue gas enters a first fixed bed adsorption tower 5 through a flue gas switching device 4, contacts with a filled porous adsorption material, and adsorbs and removes SO in the flue gas at low temperature2(ii) a When the first fixed bed adsorption tower 5 is saturated in adsorption, SO2When the penetration starts, the flue gas is switched to a second fixed bed adsorption tower 5 by a flue gas switching device 4 for SO2Adsorbing while heating or vacuumizing to perform SO on the adsorbent in the first fixed bed adsorption tower 52Desorption and regeneration of the adsorbent material. When the second fixed bed adsorption tower 5 is saturated in adsorption, SO2When the penetration starts, the flue gas is switched to the first fixed bed adsorption tower 5 after the desorption is finished through the flue gas switching device 4, and the adsorption and desorption operations are circularly carried out between the two fixed bed adsorption towers 5.
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 method is carried out. The flue gas enters a flue gas waste heat recoverer 2 after being pressurized by a flue gas induced draft fan 1, the temperature of the flue gas is reduced from 120 ℃ to 70 ℃, and hot water of 80-90 ℃ is generated at the same time and enters a heat supply pipe network; the flue gas with the temperature of 70 ℃ enters a cooling system 3, the temperature is reduced to 5 ℃ in a spray cooling mode, the 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 cooling system 3 passes through the flue gasThe switching device 4 enters a first fixed bed adsorption tower 5, and the desulfurized flue gas SO2The content is less than 1mg/Nm3And the cold flow is discharged after being recovered by the cold flow recoverer 6. When SO in the flue gas is purified after desulfurization2The content exceeds 1mg/Nm3And meanwhile, the flue gas is switched to a second fixed bed adsorption tower 5 through a flue gas switching device 4 for adsorption desulfurization. At the same time, 150 ℃ hot air is introduced into the first fixed bed adsorption tower 5 to reversely sweep the bed layer, and SO is desorbed2. And after the desorption is finished, introducing cold air to blow and sweep the cooling bed layer. When the second fixed bed adsorption tower 5 is saturated in adsorption, SO in the purified flue gas after desulfurization2The content exceeds 1mg/Nm3In the process, the flue gas is switched to the first fixed bed adsorption tower 5 again through the flue gas switching device 4 for adsorption desulfurization, and meanwhile, the second fixed bed adsorption tower 5 is subjected to desorption and cold blowing operation. The alternate switching time of the two fixed bed adsorption columns 5 is proportional to the active coke loading. When the adsorption desulfurization is carried out at 5 ℃, the sulfur capacity is 80mg/g, the switching time is set to 8 hours, and 600 tons are filled in the two fixed bed adsorption towers 5.
Example two
The second embodiment is the same as the first embodiment in the whole process flow, and the difference is that the cooling system 3 adopts a three-section spray cooling mode to cool the flue gas with the temperature of 70 ℃ after waste heat recovery 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, and the first section is cooled by cooling water; cooling the second section of spray circulating liquid by a water chiller; the third section of spray circulation liquid (calcium chloride solution) is cooled by a low-temperature refrigerating unit. The adsorption and desorption regeneration processes of the active coke in the fixed bed adsorption tower 5 are consistent with the embodiment. The difference between the second embodiment and the first embodiment is that the adsorption temperature is lower, the adsorption capacity is larger, the active coke filling amount is smaller, and the tower equipment is smaller. But the energy consumption of flue gas cooling is larger at the same time. When the adsorption desulfurization is carried out at the temperature of minus 20 ℃, the sulfur capacity is 170mg/g, the switching time is set to be 8 hours, and 280 tons of the two fixed bed adsorption towers 5 are filled.
Claims (5)
1. A fixed bed type flue gas low-temperature adsorption desulfurization system is characterized by comprising a dedusted flue gas input pipeline, a flue gas induced draft fan (1), a flue gas waste heat recoverer (2), a cooling system (3), a flue gas switching device (4), a cold energy recoverer (6), a flue gas output pipeline and a plurality of fixed bed adsorption towers (5);
the outlet of the flue gas input pipeline after dust removal is communicated with the inlet of a flue gas induced draft fan (1), the outlet of the flue gas induced draft fan (1) is communicated with the inlet of a flue gas waste heat recoverer (2), the outlet of the flue gas waste heat recoverer (2) is communicated with the inlet of a cooling system (3), the outlet of the cooling system (3) is communicated with the inlet of a flue gas switching device (4), the outlet of the flue gas switching device (4) is respectively communicated with the inlets of fixed bed adsorption towers (5), the outlet of each fixed bed adsorption tower (5) is communicated with the inlet of a cold energy recoverer (6), and the outlet of the cold energy recoverer (6) is communicated with a flue gas output pipeline;
the cooling system (3) is a two-section spray cooling structure or a three-section spray cooling structure.
2. The fixed bed type flue gas low temperature adsorption desulfurization system according to claim 1, characterized in that the number of the fixed bed adsorption towers (5) is two.
3. The fixed bed type low-temperature flue gas adsorption desulfurization system according to claim 1, wherein a fixed bed adsorption tower (5) is filled with a porous adsorption material, wherein the porous adsorption material is activated carbon, activated coke or a molecular sieve.
4. A fixed bed type low-temperature flue gas adsorption desulfurization method is characterized by comprising the following steps: the method comprises the steps that flue gas enters a flue gas induced draft fan (1) through a flue gas input pipeline after dust removal, is pressurized through the flue gas induced draft fan (1), is sent into a flue gas waste heat recoverer (2) to be cooled to-20 ℃, is sent into any fixed bed adsorption tower (5) through a flue gas switching device (4), is subjected to desulfurization treatment through the fixed bed adsorption tower (5), and is sent into a cold energy recoverer (6) to recover cold energy, and is finally discharged through a flue gas output pipeline, wherein the cold energy recovered by the cold energy recoverer (6) is used for cooling the flue gas or cooling a refrigerant of a refrigeration system.
5. The method for low-temperature adsorptive desulfurization of flue gas by using fixed bed according to claim 4, wherein SO is added during adsorption2When the penetration starts, the adsorption saturation of the fixed bed adsorption tower (5) is indicated, the flue gas is input into any other fixed bed adsorption tower (5) through the flue gas switching device (4), and the SO is carried out on the saturated fixed bed adsorption tower (5)2Desorbing by heating or vacuum desorption to obtain SO2Gas for preparing liquid SO2Sulfuric acid, sulfur and sulfates.
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Cited By (5)
| 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 |
| CN116351199A (en) * | 2023-06-01 | 2023-06-30 | 中国华能集团清洁能源技术研究院有限公司 | Adsorption module with cold energy recovery function and low-temperature adsorption system |
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