CN111729504A - Fluidized bed and moving bed coupled composite adsorption reaction device and application - Google Patents
Fluidized bed and moving bed coupled composite adsorption reaction device and application Download PDFInfo
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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
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Abstract
The invention relates to a fluidized bed and moving bed coupled composite adsorption reaction device and application, which comprises an adsorption device main body (1) and an air inlet smoke box (14) positioned at the bottom of the adsorption device main body (1), wherein a fluidized bed and a moving bed are arranged in the adsorption device main body (1), the fluidized bed comprises a Venturi acceleration pipe (11) and a fluidized bed body, the Venturi acceleration pipe (11) is positioned between the air inlet smoke box (14) and the fluidized bed body and communicated with a powder adsorbent Venturi injection device (12), the moving bed comprises a conical support sieve plate and a particle adsorbent moving bed, the particle adsorbent moving bed is arranged on the conical support sieve plate, and the conical support sieve plate is connected with a particle adsorbent conveying device (13) through a guide pipe (10). Compared with the prior art, the invention can obviously improve the utilization efficiency of the adsorbent and SO3The efficiency of removing gaseous pollutants is equal, and the dust removing function is realized, so that the smoke can be effectively removedSO3And the like gaseous contaminants.
Description
Technical Field
The invention belongs to a flue gas gaseous pollutant adsorption and removal technology in the field of environmental protection, and particularly relates to a fluidized bed and moving bed coupled composite adsorption reaction device and application thereof.
Background
The heavy nonferrous metal smelting yield of China is continuously positioned in the first place of the world for more than ten years. However, in the smelting process of heavy nonferrous metals such as lead, zinc, copper, etc., since the raw materials thereof are mainly sulfides, the smelting fumes contain sulfur oxides at a high concentration. The non-ferrous metal smelting flue gas is generally washed to reduce the temperature in the purification process, and the high-concentration SO in the flue gas3Is the main reason for generating the waste acid in the smelting flue gas washing. The treatment of washing pollution also becomes the key point and difficulty of pollution prevention in the non-ferrous metal smelting industry. Therefore, SO in the flue gas is treated by using an adsorbent before the flue gas is washed3The method can effectively collect and effectively remove the adsorbent by using the dust removal device, and can obviously reduce the generation amount of the washing waste acid. Before non-ferrous metal smelting flue gas is washed, only dust removal equipment is generally arranged, wherein an electrostatic dust removal device cannot effectively remove SO3And SO3And the bag-type dust collector is easy to form dew in the cooling process, so that the bad influence of corrosion and blockage is caused on the bag-type dust collector. The conventional electrostatic dust collection device or the cloth bag dust collection device is difficult to fully exert the SO of the adsorbent3Etc. of gaseous pollutants. Therefore, it is highly desirable to develop a method for targeting SO3The dry-type trapping device can efficiently remove gaseous pollutants.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a high-efficiency composite adsorption reaction device with coupled fluidized bed and moving bed and application thereof.
The purpose of the invention can be realized by the following technical scheme: the utility model provides a fluidized bed and compound adsorption reaction device of moving bed coupling, its characterized in that, includes the adsorption equipment main part and is located the inlet flue box of adsorption equipment main part bottom, the adsorption equipment main part in be equipped with fluidized bed and removal bed, the fluidized bed include venturi accelerating tube and the fluidized bed body, this venturi accelerating tube is located between inlet flue box and the fluidized bed body, and communicates powder adsorbent venturi injection apparatus, the removal bed include toper support sieve and particle adsorbent remove the bed, particle adsorbent remove the bed and install on toper support sieve, toper support sieve pass through honeycomb duct connection particle adsorbent conveyor.
The powder adsorbent Venturi injection device injects the powder adsorbent into the flue and adsorbs gaseous pollutants in the fluidized bed.
The particle size of the powder adsorbent is 100-325 meshes (the diameter is 0.150-0.045mm), and the powder adsorbent can have higher adsorption capacity for gaseous pollutants. The powder adsorbent can be common alkaline absorbent such as sodium carbonate, sodium bicarbonate, magnesium carbonate, magnesium oxide, calcium carbonate, calcium oxide and the like, and the adsorbent with the particle size has larger specific surface area, is absorbed more quickly and is easy to fluidize.
The inclination angle of the conical support sieve plate and the horizontal direction is 30-60 degrees, so that the particles can conveniently adsorb and move downwards at a stable speed, the size of the sieve holes is 2-3mm, the flue gas can conveniently penetrate through the sieve plate and the particle adsorbent from bottom to top, and the particle adsorbent can not fall off from the sieve plate; the aperture ratio is 20-60%, can let the flue gas pierce through the sieve easily, and its size can be adjusted according to the resistance loss.
The conical support sieve plate comprises an upper conical plate and a lower conical plate, the opening parts of the upper conical plate and the lower conical plate are in butt joint, the particle adsorbent conveying device is connected with the conical bottom of the upper conical plate, the conical bottom of the lower conical plate is connected with the flow guide pipe, and the particle adsorbent conveying device conveys the particle adsorbent to the upper conical plate.
The particle adsorbent moving bed comprises a plurality of bed bodies which are arranged in parallel up and down, each bed body is fixed on a conical support sieve plate, a height limiting ring is arranged on each bed body, the particle adsorbent moves downwards along the conical support sieve plate from top to bottom, and the thickness of the particle adsorbent falling on the particle adsorbent moving bed is kept at 20-50mm under the action of the height limiting rings. The height limiting ring is welded on the conical support plate through 4-6 support guide plates, the height of the support guide plates is 20-50mm, and the direction of the support guide plates is consistent with the radial direction of the conical plate, so that the particles can be uniformly distributed on the conical support plate according to the support guide plates in the process of moving from top to bottom, and the situations that a part of local granular adsorbents are more and a part of local granular adsorbents are not available are avoided.
The granular adsorbent is led out from the granular adsorbent moving bed through the flow guide pipe, the included angle between the flow guide pipe and the horizontal direction is 60-80 degrees, and the granular adsorbent is 5-8mm in diameter. The granular adsorbent can be common alkaline adsorbents such as sodium carbonate, sodium bicarbonate, magnesium carbonate, magnesium oxide, calcium carbonate, calcium oxide and the like, and the adsorbent with the particle size is large in particle and easy to move from top to bottom on the conical plate.
A method for purifying flue gas by adopting the fluidized bed and moving bed coupled composite adsorption reaction device comprises the following steps:
firstly, spraying a powder adsorbent into a flue, enabling the flue gas to enter a fluidized bed from an air inlet smoke box, accelerating the flue gas through a Venturi accelerating tube, enabling the flue gas to enter a fluidized bed body, enabling the flue gas to be in efficient gas-solid fluidized contact with the powder adsorbent of the fluidized bed body, returning part of materials downwards in the ascending process, forming internal circulation particle flow, strengthening gas-solid mass transfer and heat transfer, realizing efficient removal of gaseous pollutants, and discharging the adsorbed saturated powder adsorbent from the bottom of the air inlet smoke box;
secondly, the flue gas passes through a particle adsorbent moving bed on the conical support sieve plate, the gaseous pollutants in the flue gas are further adsorbed by the particle adsorbent, and meanwhile, the powder adsorbent carried by the flue gas is also intercepted by the particle adsorbent moving bed to further adsorb the gaseous pollutants;
thirdly, the granular adsorbent moving from top to bottom flows out along the flow guide pipe and returns from the top of the conical support sieve plate through the granular adsorbent conveying device to perform circulating adsorption treatment on the smoke pollutants;
and fourthly, dedusting the flue gas subjected to double adsorption of the fluidized bed and the moving bed by a cyclone separation plate, and introducing the flue gas into a subsequent flue gas purification device by an induced draft fan.
The temperature of the flue gas is 150-450 ℃.
The gas velocity of the flue gas in the fluidized bed is 4-10m/s, and the gas velocity at the venturi accelerating tube is 15-25 m/s.
Firstly, spraying a powder adsorbent into a flue, and enabling flue gas carrying the powder adsorbent to enter a reaction tower from a flue box at the bottom of the reaction tower; fluidized adsorbent particles and SO in flue gas3The gaseous pollutants are subjected to chemical reaction in the fluidizing section of the reaction tower; then the residual SO in the smoke passing through the sieve plate is continuously treated by utilizing the particle adsorbent layer moving on the conical support sieve plate3Further adsorbing the gaseous pollutants and simultaneously playing the role of a filter bed; finally, the flue gas after adsorption and filtration by the moving bed is discharged from the top, and fine dust can be removed by the cyclone separation device and then enters a subsequent purification link. The invention firstly utilizes the powder adsorbent to treat SO in a fluidized state3Preliminarily adsorbing gaseous pollutants, and then utilizing the particle adsorbent to adsorb SO in a moving state3And the gaseous pollutants are deeply adsorbed. The moving bed adsorbent can adsorb SO in the flue gas3When gaseous pollutants are involved, the powder adsorbent carried by the flue gas can be intercepted, and the SO of the flue gas can be continuously treated3Etc. to adsorb the gaseous pollutants. Meanwhile, the granular adsorbent can also flow out of the adsorption tower through a guide pipe (10) and is conveyed to the top of the moving bed through an adsorbent conveying device (13) for cyclic adsorption. The invention can obviously improve the utilization efficiency of the adsorbent and SO3The removal efficiency of gaseous pollutants is equal, and the dust removal effect is achieved, SO that SO in the flue gas can be effectively removed3And the like gaseous contaminants.
Compared with the prior art, the invention has the following advantages:
1. the invention effectively combines the fluidized bed and the moving bed, not only utilizes the powder adsorbent in the fluidized bed to carry out high-efficiency adsorption on the gaseous pollutants, but also utilizes the particle adsorbent in the moving bed to carry out deep removal on the gaseous pollutants, thereby improving the removal efficiency of the gaseous pollutants; the fluidized bed adsorption unit is adopted, the fluidized state can be realized only by using a powder adsorbent, and the fluidized bed adsorption unit has large specific surface area, high adsorption speed and high adsorption efficiency, so that the fluidized adsorption unit is arranged at the lower part to adsorb pollutants as much as possible; the particle adsorbent is arranged at the upper part, so that the powder adsorbent can be collected and recovered under the filtering and dedusting effects of the particle adsorbent, and the pollutants in the flue gas can be further adsorbed by utilizing the characteristics of the particle adsorbent, so that the deep removal is realized; the two adsorbents can be recovered and recycled, and the use efficiency of the adsorbents is improved.
2. The powder adsorbent is carried by the flue gas to enter the moving bed, is intercepted by the particle adsorbent in the moving bed, and continuously adsorbs gaseous pollutants along with the particle adsorbent in the moving bed, so that the utilization efficiency of the powder adsorbent is improved, and meanwhile, the preliminary dust removal effect is also achieved;
3. the granular adsorbent used in the invention is led out of the adsorption tower through the flow guide pipe and is thrown into the top of the adsorption tower again through the granular adsorbent conveying device, so that the flue gas pollutants can be circularly adsorbed, and the utilization efficiency of the granular adsorbent is improved.
4. The invention is suitable for the requirements of dry-type capturing and purifying treatment of gaseous pollutants in various industrial flue gases of coal burning, industrial boilers, metal smelting, cement production, petrochemical industry, waste incineration and the like.
Drawings
FIG. 1 is a schematic structural diagram of a fluidized bed-moving bed coupled composite adsorption reactor of the present invention.
Detailed Description
The invention is described in detail below with reference to specific figures and examples. The following examples will assist those skilled in the art in further understanding the invention, but are not intended to limit the invention in any way. It should be noted that variations and modifications can be made by persons skilled in the art without departing from the spirit of the invention. All falling within the scope of the present invention.
As shown in fig. 1, a composite adsorption reaction device with coupled fluidized bed and moving bed comprises an adsorption device main body 1 and an air inlet smoke box 14 located at the bottom of the adsorption device main body 1, wherein a fluidized bed and a moving bed are arranged in the adsorption device main body 1, the fluidized bed comprises a venturi accelerating tube 11 and a fluidized bed body, the venturi accelerating tube 11 is located between the air inlet smoke box 14 and the fluidized bed body and is communicated with a powder adsorbent venturi injection device 12, the moving bed comprises a conical support sieve plate and a particle adsorbent moving bed, the particle adsorbent moving bed is installed on the conical support sieve plate, and the conical support sieve plate is connected with a particle adsorbent conveying device 13 through a guide pipe 10. The conical support sieve plate comprises an upper conical plate 6 and a lower conical plate 9, the opening parts of the upper conical plate 6 and the lower conical plate 9 are in butt joint, a particle adsorbent conveying device 13 is connected with the conical bottom of the upper conical plate 6, the conical bottom of the lower conical plate 9 is connected with a flow guide pipe 10, and the particle adsorbent conveying device 13 conveys a particle adsorbent to the upper conical plate 6. The particle adsorbent moving bed comprises a plurality of bed bodies which are arranged in parallel up and down, each bed body is fixed on a conical support sieve plate, a height limiting ring is arranged on each bed body, the particle adsorbent moves downwards along the conical support sieve plate from top to bottom, and the thickness of the particle adsorbent falling on the particle adsorbent moving bed is kept at 20-50mm under the action of the height limiting rings.
Wherein, the inclination angle of the conical support sieve plate and the horizontal direction is 30-60 degrees, the size of the sieve pore is 2-3mm, and the aperture ratio is 20-60%. The lower conical plate 9 is led out of the adsorption tower through a draft tube 10 with the diameter of 100mm, the included angle between the draft tube and the horizontal direction is 60-80 degrees, and the granular adsorbent is adsorbent with the diameter of 5-8mm, so that the granular adsorbent can move conveniently. The powder adsorbent and the granular adsorbent are one or more of alkaline adsorbents such as sodium hydroxide, sodium oxide, sodium carbonate, sodium bicarbonate, magnesium hydroxide, magnesium oxide, magnesium carbonate, calcium hydroxide, calcium oxide, and calcium carbonate. The particle size of the powder adsorbent is 100-325 meshes (the diameter is 0.150-0.045mm), the diameter of the particle adsorbent is about 5-8mm, and the temperature of the flue gas is 150-450 ℃. The gas velocity of the flue gas in the fluidized bed is 4-10m/s, and the gas velocity at the venturi accelerating tube is 15-25 m/s.
Example 1
The invention utilizes a composite adsorption reaction device of a laboratory, which is coupled by a fluidized bed and a moving bed, to carry out experimental research. By rotary kilnsCalcining lead sulfide mineral powder to provide simulated non-ferrous metal smelting flue gas with the flue gas amount of 100Nm3H is used as the reference value. And (3) introducing the flue gas at the outlet of the rotary kiln into the composite adsorption reaction device with the coupled fluidized bed and moving bed after passing through the cooling device, and finally introducing the flue gas into subsequent flue gas deep evolution equipment through an induced draft fan. The temperature of the flue gas at the outlet of the cooling device downstream of the rotary kiln was maintained at 200 ℃ and SO3The concentration is 1000mg/Nm3Dust concentration of 1g/Nm3The gas velocity of the flue gas in the fluidization section is 5m/s, and the filtering velocity in the moving bed layer is 1 m/min. The moving speed of the granular adsorbent in the moving bed is 5mm/s, and the concentration of the powder adsorbent in the flue gas is 100-300mg/m3。
Example 2
The experiment was carried out using the same fluidized bed and moving bed coupled composite adsorption reactor as in example 1, and the SO in the flue gas3The concentration is 1000mg/Nm3Spraying a certain amount of powdered adsorbent (sodium bicarbonate) into the pipeline, wherein the concentration of the powdered adsorbent in the flue gas is 100mg/m3. The granular adsorbent is selected from active alumina globule (diameter of 3mm), and the moving speed of the granular adsorbent in the moving bed is 5 mm/s. The speed of the flue gas in the fluidization section is 5m/s, and the dust concentration of the flue gas is 0.05g/Nm after the flue gas passes through the composite adsorption reaction device with the coupled fluidized bed and moving bed provided by the invention at the filtering speed of the moving bed of 1m/min3，SO3The concentration is 200mg/Nm3，SO3The removal efficiency was about 80%.
Example 3
The experiment was carried out using the same fluidized bed and moving bed coupled composite adsorption reactor as in example 1, and the SO in the flue gas3The concentration is 1000mg/Nm3Spraying a certain amount of powdered adsorbent (sodium bicarbonate) into the pipeline, wherein the concentration of the powdered adsorbent in the flue gas is 200mg/m3. The granular adsorbent is selected from active alumina globule (diameter of 3mm), and the moving speed of the granular adsorbent in the moving bed is 5 mm/s. The speed of the flue gas in the fluidization section is 5m/s, and after the filtering speed of the moving bed is 1m/min and passes through the composite adsorption reaction device coupled by the fluidized bed and the moving bed, the flue gas dustThe concentration is 0.05g/Nm3，SO3The concentration is 80mg/Nm3，SO3The removal efficiency was about 92%.
Claims (10)
1. The utility model provides a fluidized bed and compound adsorption reaction device of moving bed coupling, its characterized in that, includes adsorption equipment main part (1) and is located air inlet smoke box (14) of adsorption equipment main part (1) bottom, adsorption equipment main part (1) in be equipped with fluidized bed and moving bed, the fluidized bed include venturi accelerating tube (11) and the fluidized bed body, this venturi accelerating tube (11) are located between air inlet smoke box (14) and the fluidized bed body, and communicate powder adsorbent venturi injection apparatus (12), the moving bed include toper support sieve and particle adsorbent moving bed, the particle adsorbent moving bed install on the toper support sieve, toper support sieve pass through honeycomb duct (10) and connect particle adsorbent conveyor (13).
2. The fluidized bed-moving bed coupled composite adsorption reactor of claim 1, wherein the venturi injection device (12) injects the powder adsorbent into the flue and adsorbs the gaseous pollutants in the fluidized bed.
3. The fluidized bed-moving bed coupled composite adsorption reactor as claimed in claim 2, wherein the particle size of the powder adsorbent is 100-325 mesh, which can have higher adsorption capacity for gaseous pollutants.
4. The fluidized bed-moving bed coupled composite adsorption reactor as claimed in claim 1, wherein the angle of inclination of the conical support sieve plate to the horizontal direction is 30-60 degrees, the size of the sieve hole is 2-3mm, and the opening ratio is 20-60%.
5. The fluidized bed and moving bed coupled composite adsorption reactor according to claim 1, wherein the conical support sieve plate comprises an upper conical plate (6) and a lower conical plate (9), the openings of the upper conical plate (6) and the lower conical plate (9) are butted, the granular adsorbent delivery device (13) is connected with the conical bottom of the upper conical plate (6), the conical bottom of the lower conical plate (9) is connected with the flow guide pipe (10), and the granular adsorbent delivery device (13) delivers the granular adsorbent to the upper conical plate (6).
6. The fluidized bed and moving bed coupled composite adsorption reactor as claimed in claim 5, wherein the moving bed of particulate adsorbent comprises a plurality of beds arranged in parallel up and down, each bed is fixed on a conical support sieve plate, each bed is provided with a height-limiting ring, the particulate adsorbent moves downwards along the conical support sieve plate from top to bottom, and the thickness of the particulate adsorbent falling on the moving bed of particulate adsorbent is maintained at 20-50mm under the action of the height-limiting rings.
7. The fluidized bed and moving bed coupled composite adsorption reactor according to claim 6, wherein the particulate adsorbent is discharged from the granular adsorbent moving bed through a flow guide pipe (10), the angle between the flow guide pipe (10) and the horizontal direction is 60-80 degrees, and the granular adsorbent is an adsorbent with a diameter of 5-8 mm.
8. A method for purifying flue gas by adopting the fluidized bed and moving bed coupled composite adsorption reaction device as defined in any one of claims 1 to 7, which is characterized by comprising the following steps:
firstly, spraying a powder adsorbent into a flue, enabling the flue gas to enter a fluidized bed from an air inlet smoke box (14), accelerating the flue gas through a Venturi accelerating tube (11) and enabling the flue gas to enter a fluidized bed body, enabling the flue gas to be in efficient gas-solid fluidized contact with the powder adsorbent of the fluidized bed body, returning part of materials downwards in the ascending process to form an internal circulation particle flow, strengthening gas-solid mass transfer and heat transfer, realizing efficient removal of gaseous pollutants, and discharging the adsorbed and saturated powder adsorbent from the bottom of the air inlet smoke box (14);
secondly, the flue gas passes through a particle adsorbent moving bed on the conical support sieve plate, the gaseous pollutants in the flue gas are further adsorbed by the particle adsorbent, and meanwhile, the powder adsorbent carried by the flue gas is also intercepted by the particle adsorbent moving bed to further adsorb the gaseous pollutants;
thirdly, the particle adsorbent moving from top to bottom flows out along the flow guide pipe (10) and returns from the top of the conical support sieve plate through a particle adsorbent conveying device (13) to perform circulating adsorption treatment on the smoke pollutants;
and fourthly, dedusting the flue gas subjected to double adsorption of the fluidized bed and the moving bed by a cyclone separation plate, and introducing the flue gas into a subsequent flue gas purification device by an induced draft fan.
9. The method as claimed in claim 8, wherein the flue gas temperature is 150 ℃ to 450 ℃.
10. The method for purifying flue gas by using the fluidized bed and moving bed coupled composite adsorption reactor according to claim 8, wherein the gas velocity of the flue gas in the fluidized bed is 4-10m/s, and the gas velocity at the venturi accelerating tube (11) is 15-25 m/s.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112933848A (en) * | 2021-02-26 | 2021-06-11 | 常春振 | A glance coal clarification plant for highway engineering construction usefulness |
| CN112933911A (en) * | 2021-03-08 | 2021-06-11 | 上海交通大学 | Moving bed desulfurization system based on flue gas semidry desulfurization and application thereof |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030175194A1 (en) * | 2000-08-01 | 2003-09-18 | Enviroscrub Technologies Corporation | System and process for removal of pollutants from a gas stream |
| CN1546218A (en) * | 2003-12-05 | 2004-11-17 | 清华大学 | Quick-speed fluidized bed reactor capable of realizing particles and gas back flow contact |
| CN1820819A (en) * | 2006-01-20 | 2006-08-23 | 史鱼海 | Coupling multistage device with active carbon purifying waste gas |
| CN101310831A (en) * | 2007-05-21 | 2008-11-26 | 威海市正大环保设备有限公司 | Carbon roasting smoke dust dry purification method and device |
| CN103596664A (en) * | 2011-12-22 | 2014-02-19 | Posco公司 | Apparatus for reducing carbon dioxide by using molten slag |
| CN108499315A (en) * | 2018-04-02 | 2018-09-07 | 中电环保股份有限公司 | Integrated apparatus and method for removing non-ferrous metal metallurgy relieving haperacidity sulfureous in flue gas oxide and heavy metal |
| CN111085092A (en) * | 2020-02-12 | 2020-05-01 | 福建龙净脱硫脱硝工程有限公司 | Desulfurization and dust removal device and desulfurization and dust removal method for gas boiler |
-
2020
- 2020-06-10 CN CN202010524589.0A patent/CN111729504A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030175194A1 (en) * | 2000-08-01 | 2003-09-18 | Enviroscrub Technologies Corporation | System and process for removal of pollutants from a gas stream |
| CN1546218A (en) * | 2003-12-05 | 2004-11-17 | 清华大学 | Quick-speed fluidized bed reactor capable of realizing particles and gas back flow contact |
| CN1820819A (en) * | 2006-01-20 | 2006-08-23 | 史鱼海 | Coupling multistage device with active carbon purifying waste gas |
| CN101310831A (en) * | 2007-05-21 | 2008-11-26 | 威海市正大环保设备有限公司 | Carbon roasting smoke dust dry purification method and device |
| CN103596664A (en) * | 2011-12-22 | 2014-02-19 | Posco公司 | Apparatus for reducing carbon dioxide by using molten slag |
| CN108499315A (en) * | 2018-04-02 | 2018-09-07 | 中电环保股份有限公司 | Integrated apparatus and method for removing non-ferrous metal metallurgy relieving haperacidity sulfureous in flue gas oxide and heavy metal |
| CN111085092A (en) * | 2020-02-12 | 2020-05-01 | 福建龙净脱硫脱硝工程有限公司 | Desulfurization and dust removal device and desulfurization and dust removal method for gas boiler |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112933848A (en) * | 2021-02-26 | 2021-06-11 | 常春振 | A glance coal clarification plant for highway engineering construction usefulness |
| CN112933911A (en) * | 2021-03-08 | 2021-06-11 | 上海交通大学 | Moving bed desulfurization system based on flue gas semidry desulfurization and application thereof |
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Application publication date: 20201002 |