CN110743323A - System and method for fluidized demercuration by recycling active coke - Google Patents
System and method for fluidized demercuration by recycling active coke Download PDFInfo
- Publication number
- CN110743323A CN110743323A CN201911038757.9A CN201911038757A CN110743323A CN 110743323 A CN110743323 A CN 110743323A CN 201911038757 A CN201911038757 A CN 201911038757A CN 110743323 A CN110743323 A CN 110743323A
- Authority
- CN
- China
- Prior art keywords
- coke
- fluidized bed
- desorption
- active coke
- inlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- 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
- B01D53/10—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 with dispersed adsorbents
- B01D53/12—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 with dispersed adsorbents according to the "fluidised technique"
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/60—Heavy metals or heavy metal compounds
- B01D2257/602—Mercury or mercury compounds
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Dispersion Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a system and a method for removing mercury by recycling active coke fluidization, wherein the system comprises the following components: the adsorption fluidized bed is used for providing a space for fluidized adsorption of mercury in flue gas, the bottom of the adsorption fluidized bed is provided with a flue gas inlet and an active coke inlet, and the active coke inlet is positioned above the flue gas inlet; the outlet of the first feeder is connected with the active coke inlet of the adsorption fluidized bed; the inlet of the first separator is connected with the top of the adsorption fluidized bed; a second feeder having an inlet connected to the solids outlet of the first separator; a desorption fluidized bed for providing a space for desorption of the active coke; the bottom of the first feeder is provided with a desorption gas inlet and a material inlet, the desorption gas inlet is used for being connected with a desorption gas source, and the material inlet is used for being connected with an outlet of the second feeder; and the inlet of the second separator is connected with the top outlet of the desorption fluidized bed, and the solid outlet of the second separator is connected with the first feeder through a conveying device.
Description
Technical Field
The invention belongs to the technical field of flue gas purification, relates to active coke fluidized demercuration and fluidized desorption of mercury, and particularly relates to a system and a method for recycling active coke fluidized demercuration.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
Coal is the most abundant fossil energy in China, so the total production amount of coal occupies more than 70% of the total primary energy production amount of China for a long time. And the energy consumption status of coal as a main consumption object is difficult to change for a long period of time. Heavy metal elements generated in the coal combustion process, wherein mercury is one of the heavy metal elements which are extremely harmful. Mercury is the only metal simple substance existing in a gaseous state at normal temperature, has permanently accumulated toxic substances in organisms and food chains, has great influence on the nerve development of infants, is also a global circulating heavy metal, and can have certain influence on the human ecological environment.
China mainly uses coal as energy, and the average mercury content of the coal is 0.22 mg/kg. As the control of the mercury content in the flue gas of the coal-fired power plant is still in the starting stage in China, the mercury pollution of the coal-fired power plant is particularly serious. The emission standard of the atmospheric pollutants of the thermal power plant requires that the emission of mercury and compounds thereof in a coal-fired boiler is controlled below 0.03mg/kg from 1 month and 1 day of 2015. Therefore, the development of the research on the mercury emission control technology has important significance for improving the environmental quality of China.
At present, the demercuration technology mainly comprises various control methods such as an adsorbent method, a catalytic oxidation method, plasma, photocatalysis and the like, wherein the application of an activated carbon injection technology is a relatively wide method, activated carbon has a relatively high specific surface area and a developed pore structure, and has relatively good adsorption performance on various pollutants, but the activated carbon has high operation cost and large adsorbent loss, so that the wide application of the activated carbon is limited. The active coke is also a hot spot of domestic and foreign research, the active coke is a product obtained by further activating after lignite pyrolysis, and because the active coke is not completely pyrolyzed, the active coke contains more hydrogen and oxygen functional groups inside, has more abundant pores and surface structures, and is the same as the active cokeThe active coke has loading property and oxidizing property, is an ideal smoke purifying agent with good mechanical strength, has relatively low price and is resistant to Hg0Has good adsorption effect. Researchers at home and abroad prepare the active coke with strong adsorption capacity through different modification modes, and the modified active coke invisibly increases the cost of mercury adsorption of the active coke.
In addition, the traditional flue gas demercuration method is to introduce the flue gas into a fluidized bed filled with active coke for flue gas demercuration, after the flue gas demercuration is carried out for a period of time, the adsorption efficiency of the active coke is reduced, in order to ensure the demercuration efficiency of the active coke on the flue gas, the fluidized bed needs to be stopped, then the dead coke in the fluidized bed is discharged, and fresh active coke is added. However, the demercuration of the flue gas can be influenced during the shutdown period, the excessive flue gas is difficult to have enough space for storage, and the direct discharge can cause pollution to the surrounding environment.
Disclosure of Invention
In order to solve the technical problems in the prior art, the invention aims to provide a system and a method for fluidized demercuration by recycling active coke. The system can utilize the active coke to adsorb mercury in the flue gas, then desorb the mercury, recycle the regenerated active coke again, and can continuously remove mercury from the flue gas.
In order to solve the technical problems, the technical scheme of the invention is as follows:
a system for fluidized demercuration by recycling activated coke, comprising:
the adsorption fluidized bed is used for providing a space for fluidized adsorption of mercury in flue gas, the bottom of the adsorption fluidized bed is provided with a flue gas inlet and an active coke inlet, and the active coke inlet is positioned above the flue gas inlet;
the outlet of the first feeder is connected with the active coke inlet of the adsorption fluidized bed;
the inlet of the first separator is connected with the top of the adsorption fluidized bed;
a second feeder having an inlet connected to the solids outlet of the first separator;
a desorption fluidized bed for providing a space for desorption of the active coke; the bottom of the first feeder is provided with a desorption gas inlet and a material inlet, the desorption gas inlet is used for being connected with a desorption gas source, and the material inlet is used for being connected with an outlet of the second feeder;
and the inlet of the second separator is connected with the top outlet of the desorption fluidized bed, and the solid outlet of the second separator is connected with the first feeder through a conveying device.
The invention adopts the active coke to adsorb the mercury in the flue gas in a fluidized way, the active coke has rich pores and surface structures, and contains more hydrogen and oxygen functional groups inside, thereby having better effect on the adsorption of the mercury. Meanwhile, the activated coke has better mechanical strength, is not easy to crush when flowing along with gas, and is beneficial to the subsequent gas-solid separation.
The invention adopts fluidization to adsorb mercury, so that the gas-solid contact area is large and the activity is violent, the diffusion process of substances is greatly enhanced, and the adsorption rate is improved. Meanwhile, the continuity of the demercuration process is realized, and the inconvenience brought by the replacement of the active coke is reduced. Meanwhile, fluidized desorption is used, so that the contact area of the active coke and the mixed gas is increased, the mercury on the surface of the active coke is better carried away, and a better desorption effect is achieved.
After the activated coke adsorbs mercury in the flue gas, the activated coke is desorbed in the desorption fluidized bed at the same time, and the obtained regenerated activated coke can be reused, so that the cyclic utilization of the activated coke is realized, and the cost of flue gas demercuration is reduced.
And simultaneously adding the flue gas and the active coke into the adsorption fluidized bed, controlling the flow rate of the flue gas to enable the flue gas to synchronously carry the active coke out of the adsorption fluidized bed, separating the spent coke and the desorption gas into the desorption fluidized bed synchronously after the flue gas is separated by the first separator, synchronously carrying the spent coke by controlling the flow rate of the desorption gas, and carrying out desorption and regeneration of the spent coke. The regenerated active coke is directly introduced into the adsorption fluidized bed for cyclic utilization. Through the setting of this system, can realize the cyclic utilization of active burnt, when having solved among the prior art flue gas demercuration, after the absorption fluidized bed operation a period, need shut down and carry out work again after the replacement of weary burnt, influence the problem of flue gas demercuration efficiency.
In some embodiments, the system further comprises a first bag-type dust collector, wherein an inlet of the first bag-type dust collector is connected with the gas phase outlet of the first separator.
The flue gas can carry a large amount of solid particles in the flue gas that flows from the adsorption fluidized bed after the active coke demercuration, and gas-solid separator can retrieve most solid particle separation, but is difficult to retrieve the tiny particle solid particle separation that carries in the flue gas, and during direct emission, easily causes the pollution to the surrounding environment, and first sack cleaner removes dust to the flue gas after demercuration and the gas-solid separation, can discharge after removing dust, can reduce the pollution to the surrounding environment.
In some embodiments, a spent coke collector is connected between the first separator and the second feeder.
Therefore, a spent coke collector is arranged to temporarily collect spent coke.
In some embodiments, a heat exchanger is connected between the desorption fluidized bed and the second separator, and a cold medium channel of the heat exchanger is connected with a cold water source.
The heat in the desorption gas can be transferred to cold water through the heat exchanger, and the cold water is heated, so that the heat recovery efficiency is improved.
In some embodiments, the system further comprises a regenerated activated coke collector connected between the solids outlet of the second separator and the first feeder.
A method for fluidized demercuration by recycling active coke comprises the following steps:
the active coke is fed below the adsorption fluidized bed through a first feeder and is mixed with the flue gas entering from the lower part of the adsorption fluidized bed, the mercury in the flue gas is removed, the flow rate of the flue gas is adjusted, and the active coke is synchronously carried out of the adsorption fluidized bed;
the mixture of the flue gas flowing out of the top of the adsorption fluidized bed and the active coke enters a first separator for gas-solid separation, the separated dead coke is desorbed and regenerated in a desorption fluidized bed, the flow rate of desorption gas is adjusted, and the regenerated active coke is carried synchronously;
and the mixture of the flue gas and the active coke flowing out of the desorption fluidized bed enters a second separator for gas-solid separation, and the separated regenerated active coke is circulated back to the desorption fluidized bed for flue gas demercuration.
In some embodiments, the active coke is recycled, the efficiency can reach 70-80% after 9 times of use, and the active coke is replaced after 10 times of use.
In some embodiments, the particle size of the activated coke is 80-150 μm.
In some embodiments, the adsorption temperature of the activated coke on mercury is 70-120 ℃, and the optimal adsorption temperature is 80 ℃.
In some embodiments, the flow velocity of the flue gas in the adsorption fluidized bed is 0.1-0.5 m/s. The flue gas of this velocity of flow can realize carrying active burnt synchronous, guarantees the demercuration efficiency of flue gas simultaneously.
Furthermore, in the adsorption fluidized bed, the adding amount of the active coke in each liter of flue gas is 0.5-3 g. The flue gas flow velocity is great, through the reasonable ratio of control active coke and flue gas, can guarantee the demercuration efficiency of flue gas.
Furthermore, the adsorption time of the active coke on mercury in the flue gas is 2-4 min.
Furthermore, the desorption temperature of the dead coke is 750-900 ℃, and the optimal desorption temperature is 850 ℃.
Further, the time for desorbing the dead coke is 2-4 min.
Further, the desorption gas of the spent coke desorption is a mixed gas of nitrogen and carbon dioxide or a mixed gas of nitrogen and water.
Furthermore, in the mixed gas of nitrogen and carbon dioxide, the mass percent of the carbon dioxide is 3-6%;
the mass percentage of the water vapor in the mixed gas of the nitrogen and the water is 4-8%. The active coke is obtained by incompletely activating coal, and the desorption gas is used for desorbing mercury adsorbed in the active coke and can further activate the active coke in the desorption process to improve the pore structure of the active coke.
In some embodiments, the regenerated activated coke is quantitatively and periodically added to the adsorption fluidized bed.
In some embodiments, the flow rate of the stripping gas is 0.1 to 0.5 m/s.
The invention has the beneficial effects that:
the method utilizes the active coke to adsorb mercury in the flue gas, and simultaneously desorbs in the desorption fluidized bed, so that the obtained regenerated active coke can be reused, the cyclic utilization of the active coke is realized, and the waste of resources is reduced.
The desorbed gas contains mercury, and the mercury can be purified through subsequent treatment to obtain elemental mercury, so that not only is the purification of the flue gas realized, but also the recovery of metals is realized.
The invention adopts the active coke to adsorb mercury in a fluidized manner, improves the adsorption efficiency, simultaneously keeps the flue gas and the active coke in a flowing state, and can continuously carry out the mercury removal process of the flue gas.
The invention adds a heat exchanger at the outlet of the desorption fluidized bed, thereby not only completing the cooling of the regenerated active coke, but also realizing the recovery of partial heat in the process and reducing the energy consumption in the system.
The invention uses active coke to remove mercury in a fluidized way, and the initial mercury concentration is 45 mu g/m3Maximum concentration of outlet mercury 2. mu.g/m3The mercury removal efficiency of the active coke reaches more than 95 percent.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description serve to explain the invention and not to limit the invention.
FIG. 1 is a schematic structural diagram of a system for fluidized demercuration by recycling active coke according to an embodiment of the present invention.
The system comprises a first feeder, a second feeder, an adsorption fluidized bed, a first cyclone separator, a first bag-type dust collector, a second bag-type dust collector, a spent coke collector, a second feeder, a desorption fluidized bed, a second cyclone separator, a second feeder, a regeneration active coke collector, a second bag-type dust collector, a second cyclone separator, a heat exchanger and a regeneration active coke collector, wherein the first feeder, the second feeder, the adsorption fluidized bed, the first cyclone separator, the first bag-type dust collector, the second bag-type dust.
Detailed Description
It is to be understood that the following detailed description is exemplary and is intended to provide further explanation of the invention as claimed. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the invention. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
The invention is further illustrated by the following examples:
example 1
As shown in fig. 1, the system for recycling active coke fluidized demercuration comprises: the device comprises a first feeder 1, an adsorption fluidized bed 2, a first cyclone separator 3, a first bag-type dust collector 4, a coke-depleted collector 5, a second feeder 6, a desorption fluidized bed 7, a second cyclone separator 8, a regenerated active coke collector 9, a second bag-type dust collector 10 and a heat exchanger 11. The export of first feeder 1 links to each other with the below entrance of adsorption fluidized bed 2, and the top export of adsorption fluidized bed 2 links to each other with first cyclone 3, and cyclone 3's export links to each other with 4 entrys of first sack cleaner, 5 entrys of burnt collector that lack respectively. The outlet of the coke-depleted collector 5 is connected with the inlet of a second feeder 6, and the outlet of the second feeder 6 is connected with the lower part of a desorption fluidized bed 7. An outlet of the desorption fluidized bed 7 is connected with a heat exchanger 11, an outlet of the heat exchanger 11 is connected with a second cyclone separator 8, and an outlet of the second cyclone separator 8 is respectively connected with an inlet of a second bag-type dust collector 10 and an inlet of a spent coke collector 5. The outlet of the spent coke collector 5 is connected with the first feeder 1.
Active coke with particle size of 100-120 mu m and flue gas (mercury concentration of 45 mu g/m)3) The flue gas flows from bottom to top in the adsorption fluidized bed 2, the flow rate of the flue gas is 0.2m/s, the adding amount of the active coke is 1.5g added in each liter of the flue gas, the particle size of the active coke is 80-150 mu m, the active coke adsorbs mercury in the flue gas at the temperature of 80 ℃, and the flue gas flows out after being adsorbed for 4 min. The absorbed spent coke and demercuration flue gas enter a first cyclone separator 3 for gas-solid separation, and the separated spent coke and demercuration flue gas are exhaustedThe coke enters a coke-depleted collector, and the purified flue gas is discharged by a bag-type dust collector for subsequent treatment.
The spent coke in the spent coke collector enters the desorption fluidized bed together with desorption gas (the mass percentage of the carbon dioxide in the mixed gas of the nitrogen and the carbon dioxide is 5%) from the lower part through a second feeder, the flow rate of the desorption gas is 0.2m/s, mercury on the surface of the spent coke is desorbed into the gas under the condition of 850 ℃, and the mercury flows out after the desorption for 4 min. And cooling the desorbed gas-solid mixture in a heat exchanger, and then passing through a second cyclone separator to obtain regenerated active coke and mercury-containing gas. The regenerated active coke returns to the first feeder and is sent to the adsorption fluidized bed for continuous demercuration.
In the example, the mercury removal rate of the activated coke used once is 92.1%, the mercury removal rate of the activated coke used twice in a recycling mode is 93.7%, the mercury removal rate of the activated coke used in a recycling mode for the third time is 95.2%, and the mercury removal rate of the activated coke used in a recycling mode for the fourth time is 97.6%; this time is the maximum mercury removal rate for 9 cycles of activated coke. Then the mercury removal rate of the activated coke gradually decreases, and when the cycle is carried out for the 9 th time, the mercury removal rate is 79.7%, and the activated coke is replaced.
Example 2
The system has the same structure as that in embodiment 1. The method for removing mercury from flue gas specifically comprises the following steps: active coke with particle size of 80-100 μm and flue gas (mercury concentration of 45 μ g/m)3) The flue gas flows from bottom to top in an adsorption fluidized bed, the flow rate of the flue gas is 0.4m/s, the adding amount of the active coke is 2g per liter of flue gas, the particle size of the active coke is 80-150 mu m, the active coke adsorbs mercury in the flue gas at 70 ℃, and the mercury is adsorbed for 2.5min and then flows out. And the absorbed spent coke and demercuration flue gas enter a first cyclone separator for gas-solid separation, the separated spent coke enters a spent coke collector, and the purified flue gas is discharged by a bag-type dust collector for subsequent treatment.
The spent coke in the spent coke collector enters a desorption fluidized bed together with desorption gas (the desorption gas is mixed gas of nitrogen and water, and the mass percentage of water vapor is 7%) from the lower part through a second feeder, the flow rate of the desorption gas is 0.4m/s, mercury on the surface of the spent coke is desorbed into the gas under the condition of 750 ℃, and the mercury flows out after being desorbed for 2 min. And cooling the desorbed gas-solid mixture in a heat exchanger, and then passing through a second cyclone separator to obtain regenerated active coke and mercury-containing gas. The regenerated active coke returns to the first feeder and is sent to the adsorption fluidized bed for continuous demercuration.
In this example, the mercury removal rate of activated coke used once is 91.2%, the mercury removal rate of activated coke used twice is 92.8%, the mercury removal rate of activated coke used three times is 94.0%, the mercury removal rate of activated coke used four times is 94.6%, the mercury removal rate of activated coke used five times is 95.1%, and this is the maximum mercury removal rate of activated coke cycle 9 times. And then the mercury removal rate of the activated coke is gradually reduced, and the mercury removal rate is 72.7% when the cycle is carried out for the 9 th time, and the activated coke is replaced.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A system for recycling active coke fluidization demercuration is characterized in that: the method comprises the following steps:
the adsorption fluidized bed is used for providing a space for fluidized adsorption of mercury in flue gas, the bottom of the adsorption fluidized bed is provided with a flue gas inlet and an active coke inlet, and the active coke inlet is positioned above the flue gas inlet;
the outlet of the first feeder is connected with the active coke inlet of the adsorption fluidized bed;
the inlet of the first separator is connected with the top of the adsorption fluidized bed;
a second feeder having an inlet connected to the solids outlet of the first separator;
a desorption fluidized bed for providing a space for desorption of the active coke; the bottom of the first feeder is provided with a desorption gas inlet and a material inlet, the desorption gas inlet is used for being connected with a desorption gas source, and the material inlet is used for being connected with an outlet of the second feeder;
and the inlet of the second separator is connected with the top outlet of the desorption fluidized bed, and the solid outlet of the second separator is connected with the first feeder through a conveying device.
2. The system for recycling activated coke fluidization demercuration according to claim 1, wherein: the device also comprises a first bag-type dust collector, wherein an inlet of the first bag-type dust collector is connected with a gas phase outlet of the first separator.
3. The system for recycling activated coke fluidization demercuration according to claim 1, wherein: and a spent coke collector is connected between the first separator and the second feeder.
4. The system for recycling activated coke fluidization demercuration according to claim 1, wherein: and a heat exchanger is connected between the desorption fluidized bed and the second separator, and a cold medium channel of the heat exchanger is connected with a cold water source.
5. The system for recycling activated coke fluidization demercuration according to claim 1, wherein: the device also comprises a regenerated active coke collector, and the regenerated active coke collector is connected between the solid outlet of the second separator and the first feeder.
6. A method for removing mercury by recycling active coke fluidization is characterized in that: the method comprises the following steps:
the active coke is fed below the adsorption fluidized bed through a first feeder and is mixed with the flue gas entering from the lower part of the adsorption fluidized bed, the mercury in the flue gas is removed, the flow rate of the flue gas is adjusted, and the active coke is synchronously carried out of the adsorption fluidized bed;
the mixture of the flue gas flowing out of the top of the adsorption fluidized bed and the active coke enters a first separator for gas-solid separation, the separated dead coke is desorbed and regenerated in a desorption fluidized bed, the flow rate of desorption gas is adjusted, and the regenerated active coke is carried synchronously;
and the mixture of the flue gas and the active coke flowing out of the desorption fluidized bed enters a second separator for gas-solid separation, and the separated regenerated active coke is circulated back to the desorption fluidized bed for flue gas demercuration.
7. The method for recycling activated coke fluidization demercuration according to claim 6, wherein: the particle size of the active coke is 80-150 μm;
furthermore, the adsorption temperature of the activated coke on mercury is 70-120 ℃, and the optimal adsorption temperature is 80 ℃.
Furthermore, the time for adsorbing mercury by the active coke is 2-4 min.
8. The method for recycling activated coke fluidization demercuration according to claim 6, wherein: the desorption temperature of the dead coke is 750-900 ℃, and the optimal desorption temperature is 850 ℃;
further, the time for desorbing the dead coke is 2-4 min.
9. The method for recycling activated coke fluidization demercuration according to claim 6, wherein: the desorption gas of the spent coke desorption is a mixed gas of nitrogen and carbon dioxide or a mixed gas of nitrogen and water;
furthermore, in the mixed gas of nitrogen and carbon dioxide, the mass percent of the carbon dioxide is 3-6%;
in the mixed gas of nitrogen and water, the mass percent of water vapor is 4-8%;
the flow rate of the desorption gas is 0.1 to 0.5 m/s.
10. The method for recycling activated coke fluidization demercuration according to claim 6, wherein: the flow velocity of the flue gas in the adsorption fluidized bed is 0.1-0.5 m/s, and the adding amount of the active coke in each liter of flue gas in the adsorption fluidized bed is 0.5-3 g.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911038757.9A CN110743323A (en) | 2019-10-29 | 2019-10-29 | System and method for fluidized demercuration by recycling active coke |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911038757.9A CN110743323A (en) | 2019-10-29 | 2019-10-29 | System and method for fluidized demercuration by recycling active coke |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110743323A true CN110743323A (en) | 2020-02-04 |
Family
ID=69280860
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911038757.9A Pending CN110743323A (en) | 2019-10-29 | 2019-10-29 | System and method for fluidized demercuration by recycling active coke |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110743323A (en) |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5882381A (en) * | 1996-03-28 | 1999-03-16 | Modern Equipment Company, Inc. | Thermal desorption system |
| CN1435273A (en) * | 2002-01-29 | 2003-08-13 | 国家电站燃烧工程技术研究中心 | Cyclic fluidized bed active coke desulfurating and sulfur reutilization method |
| CN201353472Y (en) * | 2009-01-08 | 2009-12-02 | 重庆大学 | Mercury removing device for smoke gas |
| CN102489116A (en) * | 2011-12-16 | 2012-06-13 | 国电环境保护研究院 | Coal flue gas mercury adsorbing removal process capable of recovering adsorbent and device utilizing same |
| CN102716635A (en) * | 2012-06-12 | 2012-10-10 | 清华大学 | Method and system for simultaneously removing heavy metals and fine particle matters in smoke |
| CN102728181A (en) * | 2012-07-23 | 2012-10-17 | 东南大学 | Fluidized bed jetting adsorbent smoke demercuration device and method thereof |
| CN104353325A (en) * | 2014-11-12 | 2015-02-18 | 上海锅炉厂有限公司 | Device and method for removing mercury from boiler flue gas of power station |
| CN105289204A (en) * | 2015-11-23 | 2016-02-03 | 金川集团股份有限公司 | System and method using powdery active cock for processing low concentration sulfur dioxide flue gas |
| CN106039929A (en) * | 2016-07-25 | 2016-10-26 | 西安热工研究院有限公司 | Circular demercuration and mercury recycling system and method for renewable adsorbent |
| CN109621899A (en) * | 2019-01-17 | 2019-04-16 | 山东大学 | A kind of preparation system and method for demercuration sulfur loading active carbon/coke |
-
2019
- 2019-10-29 CN CN201911038757.9A patent/CN110743323A/en active Pending
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5882381A (en) * | 1996-03-28 | 1999-03-16 | Modern Equipment Company, Inc. | Thermal desorption system |
| CN1435273A (en) * | 2002-01-29 | 2003-08-13 | 国家电站燃烧工程技术研究中心 | Cyclic fluidized bed active coke desulfurating and sulfur reutilization method |
| CN201353472Y (en) * | 2009-01-08 | 2009-12-02 | 重庆大学 | Mercury removing device for smoke gas |
| CN102489116A (en) * | 2011-12-16 | 2012-06-13 | 国电环境保护研究院 | Coal flue gas mercury adsorbing removal process capable of recovering adsorbent and device utilizing same |
| CN102716635A (en) * | 2012-06-12 | 2012-10-10 | 清华大学 | Method and system for simultaneously removing heavy metals and fine particle matters in smoke |
| CN102728181A (en) * | 2012-07-23 | 2012-10-17 | 东南大学 | Fluidized bed jetting adsorbent smoke demercuration device and method thereof |
| CN104353325A (en) * | 2014-11-12 | 2015-02-18 | 上海锅炉厂有限公司 | Device and method for removing mercury from boiler flue gas of power station |
| CN105289204A (en) * | 2015-11-23 | 2016-02-03 | 金川集团股份有限公司 | System and method using powdery active cock for processing low concentration sulfur dioxide flue gas |
| CN106039929A (en) * | 2016-07-25 | 2016-10-26 | 西安热工研究院有限公司 | Circular demercuration and mercury recycling system and method for renewable adsorbent |
| CN109621899A (en) * | 2019-01-17 | 2019-04-16 | 山东大学 | A kind of preparation system and method for demercuration sulfur loading active carbon/coke |
Non-Patent Citations (3)
| Title |
|---|
| 全小盾等: "《煤化学与煤分析》", 30 April 2012 * |
| 赵毅等: "《电力环境保护技术》", 31 December 2007 * |
| 郝美英等: "《矿产资源节约与综合利用鼓励、限制和淘汰技术汇编》", 31 January 2012 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103007679B (en) | Flue gas cleaning system capable of switching pollutant desorption technology and adsorbent regeneration technology and method thereof | |
| CN112063422B (en) | Blast furnace gas desulfurization and sulfur resource utilization method and device | |
| CN102350214A (en) | Coal-fired power plant coal dust prepared activated coke flue gas comprehensive purification system and technology | |
| CN102974181A (en) | Flue gas dedusting and desulfurization and denitrification craft and special device thereof | |
| CN109513311B (en) | Waste gas treatment method for realizing high-efficiency energy-saving dynamic fluidized bed graded adsorption | |
| CN101856587A (en) | Fluidized activated carbon combined desulfurization and denitrification process | |
| CN107961770B (en) | Regeneration system and regeneration method of adsorbent in coke oven flue gas purification | |
| CN106039929A (en) | Circular demercuration and mercury recycling system and method for renewable adsorbent | |
| CN107019991B (en) | CO in industrial flue gas2Enrichment and waste heat recovery system and method | |
| CN105727729A (en) | Continuous circulation carbon dioxide capture system on basis of in-situ adsorption/desorption modes | |
| CN101791506A (en) | Industrial organic exhaust gas active-carbon bed plasma integrated purification technology and device thereof | |
| CN109224803A (en) | A kind of flue gas purifying technique and device | |
| CN201586464U (en) | Large-scale active coke convection adsorption flue gas purification system | |
| CN110755999B (en) | Full-flow fluidized active coke demercuration recovery process and system | |
| CN202942787U (en) | Switchable flue gas purification system for pollutant removal process and adsorbent regeneration process | |
| CN101428189B (en) | Apparatus and method for removing inhalation particulate matter of fire coal at front body to implement zero discharge of carbonic anhydride | |
| CN108970595B (en) | Method and system for adsorption desulfurization and desorption regeneration of catalyst efficiency-improving active coke flue gas | |
| CN108970328B (en) | Device and process for treating high-sulfur waste gas in chemical industry and recovering sulfur | |
| CN102145245B (en) | Large active coke convection/adsorption gas purifying system and purifying method | |
| CN109499313A (en) | The low-temp desulfurization method of denitration of sintering flue gas | |
| CN210332252U (en) | To CO in cement kiln tail flue gas2Trapping, concentrating and utilizing system | |
| CN112322363A (en) | Nano composite zeolite adsorption blast furnace gas fine desulfurization process and device | |
| CN111470476A (en) | Method for recycling and recovering sulfur from regenerated sulfur-containing tail gas subjected to active coke dry method flue gas treatment | |
| WO2006076849A1 (en) | Cleaning process for converting a waste gas into an industrial organic waste gas capable of circulating utilization | |
| CN110743323A (en) | System and method for fluidized demercuration by recycling active coke |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200204 |
|
| RJ01 | Rejection of invention patent application after publication |