CN112933910B - Moving bed coupling absorption desulfurization method based on flue gas semidry method - Google Patents
Moving bed coupling absorption desulfurization method based on flue gas semidry method Download PDFInfo
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
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- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/508—Sulfur oxides by treating the gases with solids
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
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- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention relates to a moving bed coupling absorption desulfurization method based on a flue gas semidry method, which comprises the following steps: (1) Conveying the granular desulfurizer to a moving bed adsorption device (1), and spraying desulfurization absorption liquid to the surface of the granular desulfurizer; (2) The granular adsorbent flowing out of the moving bed adsorption device (1) passes through a vibrating screen conveying device (11), fine desulfurizer powder generated by abrasion is separated, and then the granular desulfurizer is added into the moving bed adsorption device (1) from the upper end of the moving bed adsorption device (1) through a granular desulfurizer lifting device (12) for cyclic utilization; (3) And the flue gas adsorbed by the moving bed adsorption device (1) passes through a bag-type dust collector (2) to realize flue gas desulfurization. Compared with the prior art, the invention effectively combines the wet method and the semi-dry method desulfurization process, improves the desulfurization efficiency of the flue gas, reduces the generation of desulfurization waste water, and provides a basis for the application of the subsequent low-temperature flue gas denitration technology.
Description
Technical Field
The invention relates to the technical field of flue gas gaseous pollutant adsorption and removal, in particular to a moving bed coupling absorption desulfurization method based on a flue gas semidry method.
Background
Flue Gas Desulfurization (FGD) is a major process for industrial flue gas purification. The main principle is that the alkaline absorbent/adsorbent is used for capturing sulfur dioxide in the flue gas, thereby achieving the purpose of flue gas purification. The general powder of the flue gas desulfurization process is three types of wet desulfurization, dry desulfurization and semi-dry desulfurization, wherein the wet desulfurization effect is the best, so that most industrial flue gas desulfurization adopts a wet desulfurization method. However, wet desulfurization requires a large amount of process water, and its reaction temperature is low, and clogging and corrosion of pipes and equipment are severe. The dry and semi-dry desulfurization technologies have the advantages of low investment, no sewage, low corrosion and the like, but the desulfurization efficiency is not as high as that of the wet desulfurization technology, and the control requirement of ultralow emission of industrial flue gas at present is difficult to meet.
At present, the control strength of industrial flue gas nitrogen oxides is continuously increased along with the continuous enhancement of the control strength of atmospheric pollution. Conventional SCR catalytic technology is easy to receive SO 2 The service life of the SCR catalyst is shortened due to the influence of poisoning, so that the flue gas desulfurization is a better choice before the SCR catalyst section. However, wet desulphurization can reduce the flue gas temperature and increase the SCR operation energy consumption; dry/semi-dry desulfurization is difficult to meet the requirement of ultralow emission of sulfur dioxide in flue gas, so that improvement of the existing flue gas desulfurization technology is urgently needed.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a moving bed coupling absorption desulfurization method based on a flue gas semi-dry method, which effectively combines a wet method and a semi-dry method desulfurization process, improves the desulfurization efficiency of flue gas, reduces the generation of desulfurization waste water, reduces the temperature of the flue gas less and provides a basis for the application of a subsequent flue gas low-temperature denitration technology.
The purpose of the invention can be realized by the following technical scheme:
the invention firstly provides a flue gas desulfurization system, which comprises:
moving bed adsorption device for SO in flue gas 2 Carrying out absorption;
the bag-type dust collector is used for filtering dust in the flue gas;
the particle desulfurizing agent circulating loop is used for continuously supplying particle desulfurizing agents to the moving bed adsorption device;
one end of the moving bed adsorption device is connected with the flue gas inlet, the other end of the moving bed adsorption device is connected with the bag-type dust collector, and the bag-type dust collector is also connected with the flue gas outlet.
Furthermore, the particle desulfurizer circulation loop comprises a plurality of circulating loops which are connected in sequence,
a moving bed adsorption unit;
the vibrating screen conveying device is used for separating and discharging fine desulfurizer powder generated by abrasion in the flue gas desulfurization process;
and the particle desulfurizer lifting device is used for adding the residual particle desulfurizer separated by the vibrating screen conveying device into the moving bed adsorption device for cyclic utilization.
Further, the system is also provided with a granular desulfurizer replenishing groove for replenishing fresh granular desulfurizer in the system.
Further, the system also comprises a desulfurization slurry spraying device which is used for spraying absorption components on the granular desulfurizer and is connected with the desulfurization slurry storage tank.
The invention also provides a moving bed coupling absorption desulfurization method based on a flue gas semidry method by utilizing the system, which comprises the following steps:
(1) Conveying the granular desulfurizer to a moving bed absorption device from top to bottom, and spraying desulfurization absorption liquid to the surface of the granular desulfurizer to form an absorption liquid film;
(2) In the moving bed adsorption device, the particle desulfurizer is fully contacted with the rising flue gas in the process of moving downwards to absorb SO2 in the flue gas; absorbing SO2 in the flue gas by utilizing self-surface and sprayed desulfurization absorption liquid; meanwhile, the rising hot flue gas is utilized to evaporate the water on the surface of the granular desulfurizer, and the dry desulfurizer generates fine desulfurizer powder due to abrasion in the moving process, so that deep desulfurization can be carried out, and the utilization efficiency of the desulfurizer is improved;
(3) The granular adsorbent flowing out of the moving bed adsorption device passes through a vibrating screen conveying device, fine desulfurizer powder generated by abrasion is separated, and then the granular desulfurizer is added into the moving bed adsorption device from the upper end of the moving bed adsorption device through a granular desulfurizer lifting device for cyclic utilization; the desulfurization product separated from the vibrating screen conveying device can be recycled;
(4) And the flue gas adsorbed by the moving bed adsorption device passes through a bag-type dust collector to realize flue gas desulfurization.
Further, the granular desulfurizer is conveyed to the moving bed adsorption device by a granular desulfurizer replenishing tank or a lifting device.
Further, the granular desulfurizing agent is an alkaline adsorbent, and specifically comprises one or more of magnesium oxide, calcium oxide and aluminum oxide;
the desulfurization absorption liquid is alkaline solution, and specifically comprises one or more of sodium hydroxide, sodium oxide, sodium carbonate, sodium bicarbonate, magnesium hydroxide, magnesium oxide, magnesium carbonate, calcium hydroxide, calcium oxide or calcium carbonate.
Furthermore, the diameter of the granular adsorbent is 5-8mm, and the mass concentration of the desulfurization absorption liquid is 1-20%.
The diameter of the particulate adsorbent is increased, the specific surface area in the moving bed is reduced, the contact area between the flue gas and the adsorbent particles is reduced, the removal efficiency of sulfur dioxide in the flue gas is reduced in the same retention time, and otherwise, the desulfurization efficiency is increased. However, if the diameter of the granular adsorbent is smaller, the bulk density of the adsorbent per unit volume is increased, which results in increased resistance of the flue gas passing through the moving bed, and thus the required wind pressure is increased, the power of the fan is increased, and the one-time investment and the operation energy consumption are correspondingly increased.
If the abraded particulate sorbent is not extracted, then the following three negative effects are expected: 1. since the partially worn adsorbent itself does not have desulfurization performance after multiple rounds of adsorption, the desulfurization efficiency of the whole equipment is reduced; 2. if the desulfurization product is not pumped out, the desulfurization product cannot be recovered and the adsorbent cannot be regenerated, so that the operation cost is increased; 3. the worn adsorbent has very small particle size and is easy to block a gas channel in the moving bed, and if the adsorbent is not pumped out in time, the pressure loss of equipment is increased sharply. That is, it is necessary to constantly remove a portion of the milled particulate sorbent to avoid this.
Furthermore, a sieve plate with an inclination angle of 30-50 degrees, a sieve pore size of 2-3mm and an aperture ratio of 20-60 percent is arranged in the moving bed adsorption device.
Further, the thickness of the moving bed of the granular adsorbent on the sieve plate is kept between 100 and 2000mm.
Further, the filtering speed of the flue gas passing through the moving bed adsorption device is 0.5-2.0m/min; the moving speed of the granular desulfurizing agent in the moving bed adsorption device is 5-50mm/s.
Further, the temperature of the flue gas in the moving bed adsorption device is 100-150 ℃.
In the process, the main function is to spray the absorption liquid film formed on the surface of the particulate matter, and the particulate matter adsorbent plays a role of a filler more, so the moving speed of the particulate matter adsorbent has little influence on the desulfurization efficiency. And when the flue gas temperature is lower, the desulfurization efficiency of the absorbent is higher, but insufficient heat can cause liquid accumulation in the desulfurization tower, and the design that the upper part is wet and the lower part is dry cannot be realized, so that the flue gas temperature is more proper at 100-150 ℃, and the flow of the spraying liquid and the concentration of the absorption liquid can be adjusted according to the flue gas temperature, so as to ensure the smooth implementation of the process.
Further, the liquid-gas ratio of the spraying amount of the desulfurization absorption liquid to the flue gas amount is 1-5L/m 3 。
Further, the ratio of the conveying capacity of the granular desulfurizer to the flue gas capacity is 1-20g/m 3 。
Compared with the prior art, the invention has the following advantages:
(1) The invention effectively combines the semi-dry desulfurization with the filler absorption, deeply removes gaseous pollutants by using the liquid film on the surface of the granular adsorbent, and greatly improves SO 2 The removal efficiency of (2);
(2) The invention reasonably utilizes the waste heat of the flue gas to dry the granular adsorbent, reduces the generation of desulfurization wastewater, and the adsorbent powder generated by the abrasion of the granular adsorbent in the moving process can further treat SO in the flue gas 2 To perform adsorptionTrapping improves the utilization rate of the desulfurizer;
(3) The method utilizes the vibrating screen to separate the desulfurization product from the granular adsorbent, realizes the recovery of the desulfurization product and the cyclic utilization of the granular adsorbent, and solves the problem of difficult solid-waste separation;
(4) The invention is also suitable for the requirements of dry-type capturing and purifying treatment of gaseous pollutants in various industrial flue gases such as coal burning, industrial boilers, metal smelting, cement production, petrochemical industry, waste incineration and the like.
Drawings
FIG. 1 is a schematic diagram of a flue gas desulfurization system in an example;
the reference numbers in the figures indicate: the device comprises a moving bed adsorption device 1, a vibrating screen conveying device 11, a particle desulfurizer lifting device 12, a bag-type dust remover 2 and a desulfurization slurry spraying device 3.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments.
A flue gas desulfurization system, as shown in fig. 1, comprising: moving bed adsorption device 1 for SO in flue gas 2 Carrying out absorption; the bag-type dust collector 2 is used for filtering dust in the flue gas; a granular desulfurizing agent circulation circuit for continuously supplying a granular desulfurizing agent to the moving bed adsorption apparatus 1; one end of the moving bed adsorption device 1 is connected with the flue gas inlet, the other end of the moving bed adsorption device is connected with the bag-type dust collector 2, and the bag-type dust collector 2 is also connected with the flue gas outlet. The system also comprises a desulfurization slurry spraying device 3 for spraying absorption components on the granular desulfurizer, and the desulfurization slurry spraying device 3 is connected with a desulfurization slurry storage tank. The moving bed adsorption device 1 is provided with a sieve plate with an inclination angle of 30-50 degrees, a sieve pore size of 2-3mm and an aperture ratio of 20-60 percent.
The particle desulfurizer circulation loop comprises moving bed adsorption devices 1 which are connected in sequence; the vibrating screen conveying device 11 is used for separating and discharging fine desulfurizer powder generated by abrasion in the flue gas desulfurization process; and the particle desulfurizer lifting device 12 is used for adding the residual particle desulfurizer separated by the vibrating screen conveying device 11 into the moving bed adsorption device 1 for recycling. The system is also provided with a granular desulfurizer replenishing groove for replenishing fresh granular desulfurizer in the system.
The granular desulfurizer is conveyed to the moving bed adsorption device 1 from top to bottom through the granular desulfurizer lifting device 12, and a certain amount of desulfurization slurry is sprayed on the surface of the granular desulfurizer by using a spray head of the desulfurization slurry spraying device 3 before the granular desulfurizer is conveyed to the moving bed adsorption device 1 from top to bottom; the desulfurized granular desulfurizer flows out from the bottom of the moving bed adsorption device 1, and the abraded desulfurization product is separated through the vibrating screen conveying device 11, and then the granular desulfurizer is continuously recycled.
The study is carried out by utilizing a moving bed absorption coupling device based on flue gas semi-dry desulphurization. The simulated industrial flue gas is provided by calcining pulverized coal in a rotary kiln, and the flue gas volume is 100Nm 3 H is the ratio of the total weight of the catalyst to the total weight of the catalyst. And (3) introducing the flue gas at the outlet of the rotary kiln into the moving bed absorption coupling device after passing through the cooling device, and finally introducing the flue gas into subsequent flue gas deep purification equipment through an induced draft fan. The temperature of the flue gas at the outlet of the cooling device at the downstream of the rotary kiln is maintained at 100-150 ℃ and SO 2 The concentration is 200-500mg/Nm 3 The filtering speed of the flue gas passing through the moving bed adsorption device 1 is 0.5-2.0m/min, and the moving speed of the particle adsorbent in the moving bed is 5-50mm/s.
Example 1
A moving bed coupling absorption method based on flue gas semi-dry desulfurization by using the system comprises the following steps:
(1) Conveying the granular desulfurizer to a moving bed adsorption device 1 from top to bottom, and spraying desulfurization absorption liquid to the surface of the granular desulfurizer; wherein the liquid-gas ratio of the spraying amount of the desulfurization absorption liquid to the flue gas amount is 1.0L/m 3 The ratio of the conveying amount of the granular desulfurizer to the amount of flue gas is 1g/m 3 (ii) a The desulfurization absorption liquid is magnesium carbonate with the concentration of 1 percent; the granular desulfurizer is an active alumina pellet with the grain size of about 5mm;
(2) In the moving bed adsorption device 1, the particle desulfurizer fully contacts with the rising flue gas in the process of moving downwards to remove SO in the flue gas 2 Absorbing; the self-sprayed desulfurization absorption liquid on the surface of the flue gas is utilized to remove SO in the flue gas 2 Absorbing; while utilizing rising heatThe flue gas evaporates the water on the surface of the granular desulfurizer, and the dry desulfurizer generates fine desulfurizer powder due to abrasion in the moving process, so that deep desulfurization can be carried out, and the utilization efficiency of the desulfurizer is improved; wherein, the rotary kiln provides simulated industrial flue gas by calcining coal powder, and the flue gas amount is 100Nm 3 H is used as the reference value. The flue gas at the outlet of the rotary kiln passes through a cooling device and then is introduced into a moving bed adsorption device 1, and finally the flue gas is introduced into subsequent flue gas deep purification equipment through a draught fan; the temperature of the flue gas at the outlet of the cooling device downstream of the rotary kiln was maintained at 150 ℃ and SO 2 The concentration is 500mg/Nm 3 The height of the moving bed is 1000mm. The filtering speed of the flue gas in the moving bed layer is 2m/s, and the moving speed of the particle adsorbent in the moving bed is 5mm/s. The height of the moving bed means the distance from the lowermost part of the adsorbent outlet of the main absorption column to the upper part of the whole moving bed adsorption unit 2. If the distance is high, the used adsorbent amount is large, the flue gas treatment effect is good, but the pressure loss is large; otherwise, the adsorbent is used in a small amount, the treatment effect is poor, and the pressure loss is small.
(3) The granular adsorbent flowing out of the moving bed adsorption device 1 passes through a vibrating screen conveying device 11, fine desulfurizer powder generated by abrasion is separated, and then the granular desulfurizer is added into the moving bed adsorption device 1 from the upper end of a desulfurization tower through a granular desulfurizer lifting device 12 for cyclic utilization; the desulfurization product separated from the vibrating screen conveying device 11 can be recycled;
(4) And the flue gas adsorbed by the moving bed adsorption device 1 passes through a bag-type dust collector 2 to realize flue gas desulfurization. After passing through the desulfurization system of the embodiment, SO 2 The concentration is about 30mg/Nm 3 ，SO 2 The removal efficiency was about 94%.
Example 2
A moving bed coupling absorption method based on flue gas semi-dry desulfurization by using the system comprises the following steps:
(1) Conveying the granular desulfurizer to a moving bed adsorption device 1 from top to bottom, and spraying desulfurization absorption liquid to the surface of the granular desulfurizer; wherein the desulfurization absorption liquid is sprayedThe liquid-gas ratio of the spraying amount to the smoke amount is 2.0L/m 3 The ratio of the conveying amount of the granular desulfurizer to the amount of flue gas is 1g/m 3 (ii) a The desulfurization absorption liquid is magnesium carbonate with the concentration of 1 percent; the granular desulfurizer is an active alumina pellet with the grain size of about 5mm;
(2) In the moving bed adsorption device 1, the granular desulfurizer fully contacts with the rising flue gas in the process of moving downwards to remove SO in the flue gas 2 Absorbing; the self-sprayed desulfurization absorption liquid on the surface of the flue gas is utilized to remove SO in the flue gas 2 Absorbing; meanwhile, the rising hot flue gas is utilized to evaporate the water on the surface of the granular desulfurizer, and the dry desulfurizer generates fine desulfurizer powder due to abrasion in the moving process, so that deep desulfurization can be carried out, and the utilization efficiency of the desulfurizer is improved; wherein, the rotary kiln provides simulated industrial flue gas by calcining coal powder, and the flue gas amount is 100Nm 3 H is used as the reference value. The flue gas at the outlet of the rotary kiln passes through a cooling device and then is introduced into a moving bed adsorption device 1, and finally the flue gas is introduced into subsequent flue gas deep purification equipment through a draught fan; the temperature of the flue gas at the outlet of the cooling device downstream of the rotary kiln was maintained at 150 ℃ and SO 2 The concentration is 500mg/Nm 3 The height of the moving bed is 1000mm. The filtering speed of the flue gas in the moving bed layer is 2m/s, and the moving speed of the particle adsorbent in the moving bed is 5mm/s.
(3) The granular adsorbent flowing out of the moving bed adsorption device 1 passes through a vibrating screen conveying device 11, fine desulfurizer powder generated by abrasion is separated, and then the granular desulfurizer is added into the moving bed adsorption device 1 from the upper end of a desulfurization tower through a granular desulfurizer lifting device 12 for cyclic utilization; the desulfurization product separated from the vibrating screen conveying device 11 can be recycled;
(4) And the flue gas adsorbed by the moving bed adsorption device 1 passes through a bag-type dust collector 2, so that the flue gas desulfurization is realized. After passing through the desulfurization system of the embodiment, SO 2 The concentration is about 20mg/Nm 3 ，SO 2 The removal efficiency was about 96%.
Comparative example 1
The difference from example 1 is that the diameter of the particulate adsorbent is about 1mm and the final SO 2 The removal efficiency is less than 80%. And the wind pressure can be increased, the power of the fan is increased, and the one-time investment and the operation energy consumption of the fan are correspondingly increased.
Comparative example 2
The difference from example 1 is that the diameter of the particulate adsorbent is about 20mm and the final SO 2 The removal efficiency is less than 70%.
Comparative example 3
The difference from example 1 is that the flue gas temperature at the outlet of the cooling device downstream of the rotary kiln was kept around 200 ℃, which is too close to dry desulfurization, which is inefficient and results in SO 2 The removal efficiency is less than 80%.
The foregoing is directed to preferred embodiments of the present invention, other and further embodiments of the invention may be devised without departing from the basic scope thereof, and the scope thereof is determined by the claims that follow. However, any simple modification, equivalent change and modification of the above embodiments according to the technical essence of the present invention are within the protection scope of the technical solution of the present invention.
Claims (9)
1. A moving bed coupling absorption desulfurization method based on a flue gas semidry method is characterized by comprising the following steps:
(1) Conveying the granular desulfurizer to a moving bed adsorption device (1), and spraying desulfurization absorption liquid to the surface of the granular desulfurizer; the diameter of the granular desulfurizing agent is 5-8 mm; the granular desulfurizer is an alkaline adsorbent, and specifically comprises one or more of magnesium oxide, calcium oxide or aluminum oxide; the desulfurization absorption liquid is an alkaline solution, and specifically comprises one or more of sodium hydroxide, sodium oxide, sodium carbonate, sodium bicarbonate, magnesium hydroxide, magnesium oxide, magnesium carbonate, calcium hydroxide, calcium oxide or calcium carbonate;
(2) In the moving bed adsorption device (1), the granular desulfurizer is fully contacted with the flue gas to remove SO in the flue gas 2 Absorbing;
(3) The granular desulfurizer flowing out of the moving bed adsorption device (1) passes through a vibrating screen conveying device (11), fine desulfurizer powder generated by abrasion is separated, and then the granular desulfurizer is added into the moving bed adsorption device (1) from the upper end of the moving bed adsorption device (1) through a granular desulfurizer lifting device (12) for cyclic utilization;
(4) And the flue gas adsorbed by the moving bed adsorption device (1) passes through a bag-type dust collector (2) to realize flue gas desulfurization.
2. A moving bed coupled absorption desulfurization method based on flue gas semidry process according to claim 1, characterized in that the particulate desulfurization agent is fed into the moving bed adsorption unit (1) by a particulate desulfurization agent replenishment tank or by a lift device (12).
3. The moving bed coupling absorption desulfurization method based on flue gas semidry process as claimed in claim 1, characterized in that the mass concentration of desulfurization absorption liquid is 1-20%.
4. A moving bed coupling absorption desulfurization method based on flue gas semidry process according to claim 1, characterized in that the moving bed adsorption device (1) is provided with a sieve plate with an inclination angle of 30-50 °, a sieve pore size of 2-3mm, and an aperture ratio of 20-60%.
5. The moving bed coupled absorption desulfurization method based on flue gas semidry process as claimed in claim 4, characterized in that the moving bed thickness of the particulate desulfurization agent on the sieve plate is maintained at 100-2000mm.
6. The moving bed coupling absorption desulfurization method based on flue gas semidry process according to claim 1, characterized in that the filtration speed of the flue gas passing through the moving bed adsorption device (1) is 0.5-2.0m/min; the moving speed of the granular desulfurizer in the moving bed adsorption device (1) is 5-50mm/s.
7. A moving bed coupled absorption desulfurization method based on flue gas semidry process according to claim 1, characterized in that the flue gas temperature in the moving bed adsorption device (1) is 100-150 ℃.
8. The moving bed coupling absorption desulfurization method based on the flue gas semidry method as claimed in claim 1, characterized in that the liquid-gas ratio of the spraying amount of the desulfurization absorption liquid to the flue gas amount is 1-5L/m 3 。
9. The moving bed coupling absorption desulfurization method based on flue gas semidry process as claimed in claim 1, characterized in that the ratio of the conveying capacity of the granular desulfurizing agent to the flue gas capacity is 1-20g/m 3 。
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004195394A (en) * | 2002-12-19 | 2004-07-15 | China Steel Corp | Flue gas desulfurization apparatus |
| CN110624374A (en) * | 2019-09-06 | 2019-12-31 | 江苏新中金环保科技股份有限公司 | Moving bed active coke desulfurization and denitrification system and method for recycling waste active coke powder |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2880939B2 (en) * | 1995-12-21 | 1999-04-12 | 三井鉱山株式会社 | Low temperature desulfurization method |
| NO332549B1 (en) * | 2010-12-09 | 2012-10-22 | Statoil Petroleum As | Rotary absorption wheels |
| CN202590617U (en) * | 2012-05-24 | 2012-12-12 | 首钢总公司 | Flue gas desulfurization system adopting gravity moving bed reactor |
| CN110465178B (en) * | 2018-05-09 | 2024-02-27 | 新疆北方建设集团有限公司 | Flue gas desulfurization device |
| CN111773915B (en) * | 2020-06-10 | 2022-07-15 | 上海交通大学 | Flue gas dry desulfurization process |
-
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004195394A (en) * | 2002-12-19 | 2004-07-15 | China Steel Corp | Flue gas desulfurization apparatus |
| CN110624374A (en) * | 2019-09-06 | 2019-12-31 | 江苏新中金环保科技股份有限公司 | Moving bed active coke desulfurization and denitrification system and method for recycling waste active coke powder |
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