CN109603409B - Flue gas purification system and flue gas purification method - Google Patents

Flue gas purification system and flue gas purification method Download PDF

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CN109603409B
CN109603409B CN201910002301.0A CN201910002301A CN109603409B CN 109603409 B CN109603409 B CN 109603409B CN 201910002301 A CN201910002301 A CN 201910002301A CN 109603409 B CN109603409 B CN 109603409B
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tower
flue gas
activated carbon
srg
adsorption tower
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CN109603409A (en
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魏进超
李俊杰
李勇
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Zhongye Changtian International Engineering Co Ltd
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Zhongye Changtian International Engineering Co Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/3416—Regenerating or reactivating of sorbents or filter aids comprising free carbon, e.g. activated carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/3483—Regenerating or reactivating by thermal treatment not covered by groups B01J20/3441 - B01J20/3475, e.g. by heating or cooling
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
    • B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
    • B07B1/00—Sieving, screening, sifting, or sorting solid materials using networks, gratings, grids, or the like
    • B07B1/28—Moving screens not otherwise provided for, e.g. swinging, reciprocating, rocking, tilting or wobbling screens
    • 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
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating

Abstract

A flue gas purification system comprises a desorption tower, an adsorption tower, a first conveying device, a second conveying device and a third conveying device; the analysis tower comprises a heating section, a transition section and a cooling section; an SRG gas outlet is formed in the side wall of the transition section; the top of the desorption tower is provided with a first feed inlet and a second feed inlet; an SRG gas dust removal device is arranged in the transition section and is positioned under the second feed inlet; the SRG gas dust removal device is positioned at the inner side of the SRG gas outlet, and the SRG gas dust removal device and the SRG gas outlet are tightly arranged; the first conveying device is connected with an activated carbon outlet of the adsorption tower and a first feeding hole of the desorption tower, the second conveying device is connected with an activated carbon outlet of the desorption tower and an activated carbon inlet of the adsorption tower, and the third conveying device is connected with an activated carbon outlet of the desorption tower and a second feeding hole of the desorption tower; the second feed inlet of the desorption tower is also connected with a supplementary material conveying pipeline. The invention can realize the accurate control of the active carbon material flow of the system, thereby realizing the purification of the flue gas and the dust removal of the SRG gas.

Description

Flue gas purification system and flue gas purification method
Technical Field
The invention relates to a flue gas purification system by an activated carbon method, in particular to a flue gas purification system and a flue gas purification method, and belongs to the field of environmental protection.
Background
For industrial flue gas, especially for flue gas of sintering machine in steel industry, it is desirable to use desulfurization and denitrification apparatus and process comprising activated carbon adsorption tower and desorption tower. In a desulfurization and denitration apparatus including an activated carbon adsorption tower for adsorbing pollutants including sulfur oxides, nitrogen oxides, and dioxins from sintering flue gas or exhaust gas (particularly sintering flue gas of a sintering machine in the steel industry) and a desorption tower (or regeneration tower) for thermal regeneration of activated carbon.
The activated carbon desulfurization method has the advantages of high desulfurization rate, simultaneous realization of denitration, dioxin removal, dust removal, no generation of wastewater and waste residues and the like, and is a flue gas purification method with great prospect. The activated carbon can be regenerated at high temperature, and pollutants such as sulfur oxides, nitrogen oxides, dioxin and the like adsorbed on the activated carbon are rapidly resolved or decomposed (sulfur dioxide is resolved, and nitrogen oxides and dioxin are decomposed) at the temperature of more than 350 ℃. And the regeneration speed of the activated carbon is further increased and the regeneration time is shortened with the increase of the temperature, it is preferable to generally control the regeneration temperature of the activated carbon in the desorption tower to be equal to about 430 ℃, therefore, the ideal desorption temperature (or regeneration temperature) is, for example, in the range of 390-450 ℃, more preferably in the range of 400-440 ℃.
The function of the desorption tower is to adsorb SO on the activated carbon2Releasing, decomposing more than 80% of dioxin at a temperature of more than 400 ℃ and a certain retention time, and recycling the activated carbon after cooling and screening. Released SO2Can be used for preparing sulfuric acid, etc., and the desorbed active carbon is conveyed to an adsorption tower by a conveying device for adsorbing SO2And NOx and the like.
In the adsorption tower and the desorption tower, NOx reacts with ammonia by SCR, SNCR, or the like, thereby removing NOx. The dust is adsorbed by the active carbon when passing through the adsorption tower, the vibrating screen at the bottom end of the desorption tower is separated, the active carbon powder under the screen is sent to an ash bin, and then the active carbon powder can be sent to a blast furnace or sintered to be used as fuel.
As shown in figures 1 and 2, in the process of purifying flue gas by an adsorption tower, dust in the flue gas is filtered by activated carbon in the adsorption tower, and simultaneously, a pollutant SO is generated in the flue gas2Enters the pore canal of the active carbon and is adsorbed, and the reaction is as follows:
SO2(gaseous) → SO2(adsorbed state);
SO2(adsorbed state) + H2O+1/2O2→H2SO4；
Adsorbing dust and H2SO4The active carbon is sent into the desorption tower through a conveying device, and regeneration reaction is carried out under the high-temperature condition, including H in active carbon pore channels2SO4Decomposition of (2):
Figure BDA0001934123570000011
the reaction reopens the originally blocked active carbon pore channels, but a great deal of dust is also generated due to the escape of the generated gas, and the carrier gas N in the desorption tower2The raw flue gas dust carrying the raise dust and the activated carbon adsorption is discharged from an SRG (sulfur-rich gas) outlet. Resulting in a higher SRG gas dust concentration, typically about 2g/m3The highest time can reach 10g/m3As a result, the load of subsequent sulfur-rich gas purification facilities is increased, and SO is affected2Quality of recycled products, even SO2The resource recovery process cannot be normally operated.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a flue gas purification system, wherein a feed inlet is additionally arranged on the basis of the existing feed inlet in an analytic tower in the flue gas purification system, and an SRG gas dust removal device is arranged in a transition section. When the flue gas purification system is used, the SRG gas dust removal device is filled with activated carbon, the part of activated carbon is large-particle activated carbon which is analyzed and screened and new activated carbon supplemented from the outside, the part of activated carbon does not contain or only contains little dust and easily-decomposed pollutants, and the SRG gas is dedusted by the SRG gas dust removal device before being discharged, SO that the concentration of the dust in the SRG gas is greatly reduced, the load of a sulfur-rich gas purification facility is reduced, and SO is ensured2Recycling the quality of the product.
Correspondingly, the invention also provides a flue gas purification method, and the flue gas purification method can realize accurate control of the active carbon material flow of the system, thereby realizing flue gas purification and SRG gas dust removal.
According to a first embodiment of the invention, there is provided a flue gas cleaning system:
a flue gas purification system comprises a desorption tower, an adsorption tower, a first conveying device, a second conveying device and a third conveying device. The desorption tower comprises a heating section, a transition section and a cooling section. The heating section is arranged at the upper part of the analysis tower, the cooling section is arranged at the lower part of the analysis tower, and the transition section is arranged between the heating section and the cooling section. And the side wall of the transition section is provided with an SRG gas outlet. The top of the desorption tower is provided with a first feeding hole and a second feeding hole. And an SRG gas dust removal device is arranged in the transition section and is positioned right below the second feeding hole. The SRG gas dust removal device is positioned on the inner side of the SRG gas outlet, and the SRG gas dust removal device and the SRG gas outlet are tightly arranged. The first conveying device is connected with an activated carbon outlet of the adsorption tower and a first feed inlet of the desorption tower, the second conveying device is connected with an activated carbon outlet of the desorption tower and an activated carbon inlet of the adsorption tower, and the third conveying device is connected with an activated carbon outlet of the desorption tower and a second feed inlet of the desorption tower. The bottom of the adsorption tower is provided with a first blanking valve. And a second blanking valve is arranged at the bottom of the desorption tower. The second feed inlet of the desorption tower is also connected with a supplementary material conveying pipeline.
Preferably, a first partition plate is arranged between the first feed inlet and the second feed inlet. The lower end of the first clapboard is connected with the top of the heating section.
Preferably, a second partition plate is arranged on one side of the top of the SRG gas dust removal device, and the second partition plate is arranged on the side opposite to the SRG gas outlet. The upper end of the second clapboard is connected with the bottom of the heating section, and the lower end of the second clapboard is connected with the SRG gas dust removal device.
Preferably, the first partition plate and the second partition plate are both arranged in parallel with the side where the SRG gas outlet is located, and the second partition plate is arranged right below the first partition plate.
In the invention, the SRG gas dust removal device is an activated carbon channel layer. The top and the bottom of the active carbon channel layer are both of an open structure.
Preferably, the left side and the right side of the SRG gas dust removal device are respectively of a shutter structure or a porous plate structure.
In the invention, an SRG gas collecting device is arranged in the transition section. The SRG gas dust removal device is arranged between the SRG gas collecting device and the SRG gas outlet.
The left side and the right side of the SRG gas dust removal device refer to the gas inlet end and the gas outlet end of the SRG gas dust removal device. The air inlet end of the SRG gas dust removal device is communicated with the SRG gas collecting device, and the air outlet end of the SRG gas dust removal device is communicated with the SRG gas outlet.
Preferably, the SRG gas collection assembly comprises a support plate and a plurality of activated carbon flow-through channels connected to the bottom surface of the support plate. Gaps are reserved among the activated carbon flow channels, and the gaps are SRG gas flow channels. The top and the bottom of the activated carbon flow channel are both of an open structure. The top of the SRG gas flow channel is a bearing plate, and the bottom of the SRG gas flow channel is of an open structure.
Preferably, the top of the adsorption tower is provided with a first level indicator. And a second level indicator is arranged at the first feed inlet of the desorption tower. And a third level indicator is arranged at a second feed inlet of the desorption tower.
Preferably, the lower part of the second blanking valve is provided with a vibrating screen.
According to a second embodiment of the present invention, there is provided a method of purifying flue gas:
a method of cleaning flue gas using the above flue gas cleaning system, the method comprising the steps of:
1) the raw flue gas is conveyed into an adsorption tower through a flue gas inlet of the activated carbon adsorption tower, the activated carbon adsorption of the adsorption tower treats the raw flue gas, and pollutants in the raw flue gas are adsorbed by the activated carbon in the adsorption tower; the treated flue gas is discharged from a flue gas outlet of the adsorption tower;
2) the active carbon adsorbed with the pollutants in the adsorption tower is discharged through a first blanking valve at the bottom of the adsorption tower, then is conveyed to a first feeding hole of the desorption tower through a first conveying device, is heated and regenerated in the desorption tower, and is discharged through a second blanking valve at the bottom of the desorption tower;
3) the active carbon discharged from the desorption tower is divided into two parts; one part of the smoke is conveyed to an activated carbon inlet of the adsorption tower through a second conveying device, and the original smoke is subjected to cyclic adsorption treatment; and the other part of the SRG gas is conveyed to a second feeding hole of the desorption tower through a third conveying device and then enters an SRG gas dust removal device, the activated carbon is used for removing dust in the SRG gas, and the SRG gas collected by the SRG gas collecting device is discharged from an SRG gas outlet after being subjected to dust removal by the SRG gas dust removal device.
Preferably, step 2) further comprises: and after the activated carbon discharged from the desorption tower is screened by a vibrating screen, removing dust particles in the activated carbon, and then conveying the activated carbon to an activated carbon inlet of the adsorption tower through a second conveying device and conveying the activated carbon to a second feeding hole of the desorption tower through a third conveying device.
In the present invention, the method further comprises: and 4) supplementing new active carbon from a second feeding hole of the desorption tower through a supplement conveying pipeline to enter the desorption tower according to the amount of the active carbon required by the treatment of the raw flue gas in the adsorption tower, the treatment amount of the desorption active carbon in the desorption tower and the amount of the active carbon dust removed by screening of the vibrating screen.
In the invention, the step 4) is specifically as follows:
a) detecting the raw flue gas entering the adsorption tower, calculating the amount of the activated carbon required by the raw flue gas in the adsorption tower by combining the pollutant removal efficiency requirement, and obtaining the blanking amount M of the adsorption tower1；
b) According to the relation between the frequency of the first blanking valve and the blanking amount of the adsorption tower, the frequency of the first blanking valve is adjusted to be equal to the blanking amount M of the adsorption tower1Corresponding frequency f1；
c) Setting a target material level L of a second material level meter below a first feeding hole of the analysis towerObject 2Reading the level L of the second level indicator2According to L2And LObject 2The frequency f of the second blanking valve is adjusted2So that L is2＝LObject 2；
d) According to the relation between the frequency of the second blanking valve and the blanking amount of the analysis tower, the blanking amount of the analysis tower and the frequency f of the second blanking valve are obtained2Corresponding blanking amount M2；
e) Determining the flow M of the screened outer-discharge activated carbon of a vibrating screen below the desorption towerOuter dischargeWhereby the total flow rate M of the activated carbon is fed by the second and third feeding devices2'＝M2-MOuter discharge(ii) a Keeping the feeding amount of the second conveying device to the adsorption tower at M1The feeding amount M of the third conveying device to the second feeding hole of the desorption tower3＝M2'-M1；
f) Setting a target material level L of a third material level meter below a second feeding hole of the analysis towerTarget 3Reading the level L of the third level indicator3When L is present3＜LTarget 3In the process, new active carbon is supplemented to a second feeding hole of the desorption tower through a supplement material conveying pipeline; when L is3＞LTarget 3Stopping supplementing new active carbon into the desorption tower; finally make L3＝LTarget 3。
In the invention, the raw flue gas entering the adsorption tower is detected in the step a), the amount of the activated carbon required by the raw flue gas treated in the adsorption tower is calculated, and the feed amount M of the adsorption tower is obtained1The method specifically comprises the following steps:
calculating SO to be treated by adsorption tower2Amount of NOx: detecting the flow of the original flue gas as Q and the concentration of sulfur dioxide in the original flue gas as
Figure BDA0001934123570000043
The concentration of nitrogen oxides in the raw flue gas is CNOxThus, adsorption of SO to be treated by the column2The amounts of NOx are:
Figure BDA0001934123570000042
WNOx＝ηNOx×Q×CNOx/106；………(2)
in the formula (1), the reaction mixture is,
Figure BDA0001934123570000044
SO to be treated for adsorption tower2The amount of (2) is unit kg/h; q is the flow of the original flue gas in Nm3/h；
Figure BDA0001934123570000051
Is SO in the original flue gas2Concentration of (2) in mg/Nm3；
Figure BDA0001934123570000053
Is SO2The removal efficiency of (2); in the formula (2), WNOxThe unit kg/h is the amount of NOx to be treated by the adsorption tower; cNOxFor nitrogen oxides in raw flue gasConcentration in mg/Nm3；ηNOxEfficiency of NOx removal;
based on
Figure BDA0001934123570000054
And WNOxCalculating the feed amount M of the adsorption tower1：
Figure BDA0001934123570000055
In formula (3), M1The unit kg/h is the blanking amount of the adsorption tower; k is a radical of1Is the first coefficient, k1A value of 5 to 50, preferably 8 to 40, more preferably 10 to 20; k is a radical of2Is the second coefficient, k2Values of 1 to 40, preferably 3 to 30, more preferably 5 to 20.
In the invention, the frequency f of the first blanking valve (9) in step b) is1The amount of the feed M to the adsorption tower (8)1The relationship (c) is specifically as follows: m1＝f1×k4×l1×d1 room×ρ1/r1×d1 straightWherein: k is a radical of4Fourth coefficient, l1Is the length of the first blanking valve round roller, d1 roomIs the gap of the first blanking valve round roller, rho1Is the bulk density of activated carbon in the adsorption tower, r1Maximum rotational speed of the first discharge valve round roll, d1 straightThe diameter of the first blanking valve round roller; k is a radical of4The value is 0.01 to 0.2, preferably 0.03 to 0.15, more preferably 0.05 to 0.1.
In the invention, the frequency f of the second discharge valve (10) in step d) is2The amount of feed M to the analytical column (A)2The relationship (c) is specifically as follows: m2＝f2×k5×l2×d2 room×ρ2/r2×d2 straightWherein: k is a radical of5Fifth coefficient, l2Length of the second discharge valve round roll, d2 roomIs the gap of the second blanking valve round roller, rho2To resolve the bulk density of the activated carbon in the column, r2Maximum rotational speed of the second discharge valve round roll, d2 straightIs a second blanking valveThe diameter of the round roller; k is a radical of5The value is 0.01 to 0.2, preferably 0.03 to 0.15, more preferably 0.05 to 0.1.
In the present invention, the frequency f of the second blanking valve is adjusted in step c)2The method specifically comprises the following steps:
when L is2＞LObject 2While increasing the frequency f of the second discharge valve2(ii) a When L is2＜LObject 2While reducing the frequency f of the second discharge valve2Finally make L2＝LObject 2。
In the invention, the flow M of the externally discharged activated carbon of the desorption tower is determined in the step e)Outer dischargeThe method specifically comprises the following steps:
Mouter discharge＝k3×M2；………(4)
And satisfies the following conditions: d2/(d1+d2)＞k3；………(5)
In the formula (4), k3The third coefficient is the value range of 1-3%; m2The unit kg/h is the blanking amount of the resolving tower; in the formula (5), d1The width between the inner wall of the desorption tower and the first partition plate is close to one side under the first feed inlet; d2The width of the SRG gas dust removal device is the width between the second partition plate and the SRG gas outlet, namely the width of the SRG gas dust removal device is close to one side right below the second feeding hole.
In the present invention, the first and second conveying devices may be conveyors; for example, conveyor belts are selected as the first conveyor and the second conveyor. The third conveying device can be a conveyor or a transmission device without a power device; for example, a conveyor belt or a chute may be selected as the third conveying means.
In the present invention, the second conveying device may be provided with two feed openings, wherein one feed opening supplies the adsorption tower and the other feed opening supplies the third conveying device. The third conveying device is connected with a feed opening of the second conveying device and a second feed opening of the desorption tower.
In the flue gas purification system, the top of the desorption tower is provided with a first feeding hole and a second feeding hole. And an SRG gas dust removal device is arranged in the transition section right below the second feed port, the SRG gas dust removal device is positioned on the inner side of the SRG gas outlet, and the SRG gas dust removal device and the SRG gas outlet are tightly arranged. In the invention, the SRG gas dust removal device is preferably an activated carbon channel layer, and the gas inlet end and the gas outlet end of the activated carbon channel layer are respectively in a shutter or porous plate structure. Furthermore, the louvered or perforated plate structure of the inlet end and/or the outlet end may be provided as one or more layers. Preferably, a first partition plate is further arranged between the first feeding hole and the second feeding hole, and the lower end of the first partition plate is connected with the top of the heating section. A second partition plate is further arranged on one side (namely the side opposite to the SRG gas outlet) of the top of the SRG gas dust removal device, the upper end of the second partition plate is connected with the bottom of the heating section, and the lower end of the second partition plate is connected with the SRG gas dust removal device. The first partition plate and the second partition plate are arranged in parallel with the side face where the SRG gas outlet is located, and the second partition plate is arranged under the first partition plate. In the invention, the first feeding hole and the second feeding hole of the desorption tower are separated by the first partition plate, and meanwhile, the second partition plate is additionally arranged, so that the activated carbon entering from the first feeding hole and the second feeding hole forms two material flows from top to bottom. The active carbon entering from the first feeding hole is the active carbon to be analyzed and adsorbing pollutants, the part of the active carbon is utilized, the filtering and purifying functions of the part of the active carbon are limited, and the part of the active carbon can generate a large amount of dust, so that the dust removal of SRG gas is not facilitated. The activated carbon entering from the second feeding hole is analyzed and then screened large-particle activated carbon and new activated carbon added through a supplement material conveying pipeline, the part of activated carbon does not contain or only contains little dust and easily-decomposed pollutants, the part of activated carbon does not generate dust, and dust removal of SRG gas can be better realized.
The inventor of the application researches and designs a desorption tower device, and particularly divides the active carbon entering the desorption tower into two parts in the desorption tower. One part of the gas normally passes through the heating section, the SRG gas collecting device in the transition section and the cooling section and is then discharged from the outlet; the other part passes through the heating section, the SRG dust removal device in the transition section and the cooling section and is then discharged from the outlet. However, it was found through experiments and use that this analysis was usedThe tower device, owing to the active carbon that has adsorbed the pollutant (including sulfur dioxide, nitride, dust) through the active carbon in the desorption tower, import this type of active carbon from the feed inlet of desorption tower, have following problem: 1. the active carbon entering the SRG dust removal device in the transition section contains too much dust and easily decomposed pollutants, namely a large amount of raised dust is generated, and the active carbon cannot well remove dust of SRG gas; 2. the active carbon which adsorbs pollutants (including sulfur dioxide and nitride) is arranged at the position of the SRG dust removal device, because the SRG gas has relatively large flow, the whole analysis tower discharges materials simultaneously, the active carbon passing through the SRG dust removal device cannot be fully analyzed, and the pollutants in the active carbon cannot be completely analyzed, so that the pollutants cannot be discharged from an SRG gas outlet, and the pollutants which are not analyzed are discharged from a discharge outlet of the analysis tower along with the active carbon to influence the utilization of the active carbon in the next cycle; 3. because the SRG dust removal device can not play a good role in removing dust from the SRG gas, a large amount of dust is contained in the gas discharged from the SRG gas outlet, the load of a subsequent sulfur-rich gas purification facility is increased, and SO is influenced2Recycling the quality of the product.
Through continuous research and experiments of the inventor, the novel analysis tower provided by the invention is developed, the structure of the existing analysis tower is changed, two activated carbon inlets are arranged, and the space in the analysis tower above the horizontal position of the SRG gas outlet is divided into two chambers. Referring to the drawing, the activated carbon adsorbed with the contaminants, that is, the activated carbon discharged from the adsorption tower is supplied to the left chamber (from the first supply port), and the chamber is used exclusively for desorption of the activated carbon adsorbed with the contaminants. Fresh activated carbon, namely activated carbon resolved by the resolving tower is input into a chamber on the right side (from the second feed inlet), an activated carbon layer is formed in the chamber through a shutter or a porous plate and the like to form an SRG gas dust removal device, and the chamber is used for removing dust from the SRG gas. The SRG gas dust removal device is positioned between the SRG gas collecting device and the SRG gas outlet, and SRG gas collected in the left chamber by the SRG gas collecting device passes through the SRG gas dust removal device and then is discharged from the SRG gas outlet. The SRG gas dust removal device removes dust to SRG gas by using active carbon as a filter material, the active carbon in the SRG gas dust removal device is fresh active carbon and does not adsorb pollutants, dust and the like, and the active carbon is the active carbon which only adsorbs the dust after passing through the SRG gas dust removal device, is discharged from a discharge hole of an analytical tower after passing through a cooling section and can be conveyed to the adsorption tower for cyclic utilization.
The invention divides the feed inlet of the analysis tower into two parts, and also divides the upper half part (from the feed inlet to the SRG gas outlet) of the analysis tower into two parts, wherein the activated carbon layer for dust removal forms an SRG gas dust removal device, and the activated carbon is fresh activated carbon, thereby solving the problems that the dust removal effect of the activated carbon is limited and pollutants are difficult to analyze in the prior art; the activated carbon is skillfully used as a filtering material to remove dust; meanwhile, the next recycling of the activated carbon is not influenced.
The flue gas purification system provided by the invention comprises the desorption tower, and further comprises an adsorption tower, a first conveying device, a second conveying device and a third conveying device. The first conveying device is used for conveying the pollutant-adsorbed activated carbon discharged from an activated carbon outlet of the adsorption tower to a first feeding hole of the desorption tower, the second conveying device is used for conveying the regenerated activated carbon discharged from an activated carbon outlet of the desorption tower to an activated carbon inlet of the adsorption tower, and the third conveying device is used for conveying the regenerated activated carbon discharged from an activated carbon outlet of the desorption tower to a second feeding hole of the desorption tower. The second feed inlet of the desorption tower is also connected with a supplementary material conveying pipeline. The top of the adsorption tower is provided with a first level indicator, and the first feed inlet and the second feed inlet of the desorption tower are respectively provided with a second level indicator and a third level indicator.
Correspondingly, the invention also provides a flue gas purification method based on the flue gas purification system, and the method sets the target material levels of the second material level indicator and the third material level indicator to be L respectivelyObject 2、LTarget 3And reading the actual material level L of the second material level meter and the third material level meter2、L3Adjusting according to the relation between the actual material level and the target material level of each material level meter so that L2＝LObject 2，L3＝LTarget3Thereby realizing the accurate control of the active carbon material flow and leading the whole flue gas purification system to operate organically and normally. The control method specifically comprises the following steps: firstly, the raw flue gas is detected, and SO to be processed by the adsorption tower is calculated2Calculating the amount of NOx to obtain the feed amount M of the adsorption tower1Then according to the feed amount M of the adsorption tower1Obtaining the blanking frequency f of the first blanking valve1(ii) a Then according to L2And LObject 2The blanking frequency f of the second blanking valve is obtained by adjusting the size relation2Thereby obtaining the blanking amount M of the analysis tower2(ii) a Then determining the flow M of the discharged activated carbon of the desorption towerOuter dischargeWhile keeping the material level of the adsorption tower constant, i.e. keeping the feeding amount of the second conveying device to the adsorption tower at M1Thereby obtaining the feeding amount M of the third conveying device to the second feeding hole of the desorption tower3＝M2'-M1(ii) a At the same time, when L3＜LTarget 3In the process, new active carbon is supplemented to a second feeding hole of the desorption tower through a supplement material conveying pipeline; when L is3＞LTarget 3Stopping supplementing new active carbon into the desorption tower; finally make L3＝LTarget 3。
Wherein, the flow M of the discharged activated carbon of the desorption towerOuter discharge＝k3×M2(ii) a And d is2/(d1+d2)＞k3。k3Is the third coefficient, and the value range is 1 to 3 percent. d1Is close to one side under the first feeding hole, and the width between the inner wall of the desorption tower and the first clapboard (or the second clapboard). d2The width of the SRG gas dust removal device is the width between the second partition plate (or the first partition plate) and the SRG gas outlet on the side close to the right lower part of the second feeding hole.
In the technical scheme of the invention, the operation of the activated carbon in each device is reasonably controlled, so that the whole flue gas treatment system organically and normally operates, and the accurate control of material flow is realized. The method specifically comprises the following steps: firstly, calculating the amount of active carbon required by the treatment of the flue gas amount in the adsorption tower according to the components and the content of pollutants in the raw flue gas, and controlling the frequency of a discharge valve (a first discharge valve) of the adsorption tower according to the required amount of the active carbon, so that the active carbon in the adsorption tower can effectively treat the raw flue gas in time; then the active carbon adsorbed with the pollutants in the adsorption tower is conveyed to an analysis tower for analysis treatment, and the active carbon adsorbed with the pollutants is completely conveyed to a first feeding hole of the analysis tower and then is heated for analysis; discharging the heated and desorbed fresh activated carbon from a discharge hole of the desorption tower; the active carbon (the active carbon is fresh active carbon with adsorption function) discharged from the discharge hole of the desorption tower is divided into two parts, one part is conveyed to the adsorption tower, and the original flue gas is treated by cyclic adsorption; and the other part of the SRG gas is conveyed to a second feeding hole of the desorption tower and then enters the SRG gas dust removal device for removing dust of the SRG gas. Controlling the discharge amount of the activated carbon at the discharge hole of the analysis tower according to the material level condition of a material level meter below a first feed hole in the analysis tower, and controlling the frequency of a discharge valve (a second discharge valve) of the analysis tower according to the amount of the activated carbon discharged from the discharge hole of the analysis tower as required to ensure the material level below the first feed hole in the analysis tower to be stable; and controlling the activated carbon (preferably screened total activated carbon) discharged from the discharge hole of the desorption tower, keeping the same (or equal) amount of the activated carbon conveyed to the adsorption tower as the amount of the activated carbon required in the adsorption tower, conveying the rest of the activated carbon discharged from the discharge hole of the desorption tower to the second feed hole of the desorption tower, and supplementing new activated carbon (the activated carbon is externally supplemented additional new activated carbon) in real time according to the material level condition of a material level meter below the second feed hole of the desorption tower so that the material level below the second feed hole of the desorption tower is normal.
Preferably, the activated carbon discharged from the discharge port of the desorption tower is screened by a vibrating screen and then is divided into two parts, one part is conveyed to the adsorption tower, and the other part is conveyed to the second feed port of the desorption tower. Through screening, remove the dust granule in the active carbon, improve the effect and the efficiency of active carbon in adsorption tower and SRG gas dust collector.
In the invention, the air inlet end or the air outlet end of the SRG gas dust removal device (namely the activated carbon channel layer) is respectively and independently of a shutter structure or a porous plate structure. That is, the thickness of the activated carbon passage layer, i.e., the straight distance of the gas passing through the activated carbon passage layer, is defined by the distance between the front and rear louver structures or the porous plate structure.
In the invention, the top and the bottom of the activated carbon channel layer are both of an open structure. The upper opening is communicated with the heating section, and the lower opening is communicated with the cooling section.
In the invention, the SRG gas collection assembly comprises a carrier plate and voids between a plurality of activated carbon flow channels connected at the bottom surface of the carrier plate. The top and the bottom of the activated carbon flow channel are both of an open structure. In general, the cross-section of the activated carbon flow channels is circular or rectangular or triangular. For example, the activated carbon flow channels are in the form of standpipe.
In the present invention, the length of the activated carbon flow channel is 5 to 100cm, preferably 10 to 80cm, and more preferably 15 to 60 cm.
In the invention, a plurality of activated carbon flow channels are arranged on the bearing plate, and gaps are arranged among the activated carbon flow channels. The gaps among the activated carbon flow channels are SRG gas flow channels. Sulfur-rich gas (SRG) is collected or collected within the SRG gas flow channels.
In the present invention, the cross-sectional area of the activated carbon passage layer is 1 to 20%, preferably 3 to 15%, more preferably 5 to 10% of the cross-sectional area of the SRG gas collecting apparatus.
In the invention, the heating section is of a shell-and-tube type structure; the active carbon passes through the tube pass, and the heating gas passes through the shell pass.
In the invention, the cooling section is of a shell-and-tube type structure; the active carbon passes through the tube side, and the cooling gas passes through the shell side.
In the invention, the length of the activated carbon flow-through channel is its length in the vertical direction.
In the invention, the bearing plate is provided with a plurality of activated carbon circulation channels, the number of the activated carbon circulation channels is not limited, and the activated carbon circulation channels are set according to the requirements of an actual production process and are generally designed according to factors such as the size, the resolving power, the content of pollutants in the activated carbon and the like of the resolving tower. Generally, the number of the activated carbon flow channels in the desorption tower is 50-700, preferably 100-.
In the present invention, the cross-sectional area of the activated carbon passage layer means the cross-sectional area of the activated carbon passage on the transverse face of the analytical tower. Similarly, the cross-sectional area of the SRG gas collection device refers to the cross-sectional area of the SRG gas collection device on the transverse face of the desorption tower. The cross section area of the active carbon channel layer and the size of the cross section area of the SRG gas collecting device are not limited and are set according to the requirements of the actual production process; generally according to the dust content of the SRG gas; if the dust content in the SRG gas is high, the cross-sectional area of the activated carbon channel layer is large (or the thickness of the activated carbon channel layer is larger); in contrast, if the dust content in the SRG gas is low, the cross-sectional area of the activated carbon passage layer is small (or its thickness is small).
In the present invention, the height of the stripping column is from 15 to 80m, preferably from 18 to 60m, more preferably from 20 to 40 m. Width (i.e. d) of SRG gas dust removal device2) Is 50-500mm, preferably 80-400mm, more preferably 100-300 mm. Compared with the prior art, the invention has the following beneficial technical effects:
1. according to the desorption tower in the flue gas purification system, the feed inlet is additionally arranged on the basis of the existing feed inlet, and the SRG gas dust removal device is arranged in the transition section right below the additionally arranged feed inlet, so that the dust removal of SRG gas is realized by effectively utilizing the filtering and purifying functions of fresh active carbon which is sieved after desorption and new active carbon which is supplemented from the outside;
2. according to the desorption tower in the flue gas purification system, the first partition plate is arranged between the first feed port and the second feed port, the second partition plate is arranged under the first partition plate, and the arrangement of the partition plates enables the activated carbon entering from different feed ports to form two material flows, so that the activated carbon loaded with pollutants is separated from clean activated carbon, on one hand, the activated carbon entering from the first feed port is not influenced to be desorbed and regenerated, on the other hand, the activated carbon entering from the second feed port does not generate dust or pollutants in the dust removal process, and the dust removal effect is better;
3. by adopting the flue gas purification system and the control method thereof, the accurate control of the active carbon material flow of the system can be realized, and further the purification of flue gas and the dust removal of SRG gas are realized;
4. through the desorption tower or the flue gas purification system of the inventionThe SRG gas discharged from the system has low dust content, reduces the load of sulfur-rich gas purification facilities, and ensures SO2Recycling the quality of the product.
Drawings
FIG. 1 is a schematic diagram of a prior art activated carbon flue gas purification system;
FIG. 2 is a cross-sectional view taken at location B-B of FIG. 1;
FIG. 3 is a schematic view of a desorption column according to the present invention;
FIG. 4 is a schematic diagram of the flue gas purification system of the present invention;
fig. 5 is a cross-sectional view taken at the position C-C in fig. 4.
Reference numerals: a: a resolution tower; a01: a first feed port; a02: a second feed port; 1: a heating section; 2: a transition section; 201: an SRG gas outlet; 3: a cooling section; 4: SRG gas dust removal device; 5: a first separator; 6: a second separator; 7: an SRG gas collecting device; 701: a carrier plate; 702: an activated carbon flow channel; 703: an SRG gas flow channel; 8: an adsorption tower; 9: a first baiting valve; 10: a second discharge valve; 11: a first level indicator; 12: a second level gauge; 13: a third level gauge; 14: vibrating screen; d1: a first conveying device; d2: a second conveying device; d3: a third conveying device; l: and a supplementary material conveying pipeline.
Detailed Description
According to a first embodiment of the invention, there is provided a flue gas cleaning system:
a flue gas purification system comprises a desorption tower A, an adsorption tower 8, a first conveying device D1, a second conveying device D2 and a third conveying device D3. The desorption tower A comprises a heating section 1, a transition section 2 and a cooling section 3. The heating section 1 is arranged at the upper part of the analysis tower A, the cooling section 3 is arranged at the lower part of the analysis tower A, and the transition section 2 is arranged between the heating section 1 and the cooling section 3. The side wall of the transition section 2 is provided with an SRG gas outlet 201. The top of the desorption tower A is provided with a first feed inlet A01 and a second feed inlet A02. And an SRG gas dust removal device 4 is arranged in the transition section 2 and is positioned right below the second feeding hole A02. The SRG gas dust removal device 4 is located at the inner side of the SRG gas outlet 201, and the SRG gas dust removal device 4 and the SRG gas outlet 201 are tightly arranged. The first conveying device D1 is connected with the activated carbon outlet of the adsorption tower 8 and the first feed inlet A01 of the desorption tower A, the second conveying device D2 is connected with the activated carbon outlet of the desorption tower A and the activated carbon inlet of the adsorption tower 8, and the third conveying device D3 is connected with the activated carbon outlet of the desorption tower A and the second feed inlet A02 of the desorption tower A. The bottom of the adsorption tower 8 is provided with a first blanking valve 9. The bottom of the desorption tower A is provided with a second blanking valve 10. The second feed inlet a02 of the stripper column a is also connected to a make-up feed conveying line L.
Preferably, a first partition 5 is provided between the first feed opening a01 and the second feed opening a 02. The lower end of the first partition plate 5 is connected with the top of the heating section 1.
Preferably, a second partition plate 6 is provided at a top side of the SRG gas dust removing device 4, and the second partition plate 6 is provided at a side opposite to the SRG gas outlet 201. The upper end of the second clapboard 6 is connected with the bottom of the heating section 1, and the lower end is connected with the SRG gas dust removal device 4.
Preferably, the first partition plate 5 and the second partition plate 6 are both disposed in parallel with the side where the SRG gas outlet 201 is located, and the second partition plate 6 is disposed directly below the first partition plate 5.
In the invention, the SRG gas dust removal device 4 is an activated carbon channel layer. The top and the bottom of the active carbon channel layer are both of an open structure.
Preferably, the left and right sides of the SRG gas dust removing device 4 are respectively in a louver structure or a porous plate structure.
In the present invention, an SRG gas collector 7 is provided in the transition section 2. The SRG gas dust removal device 4 is arranged between the SRG gas collecting device 7 and the SRG gas outlet 201.
Preferably, the SRG gas collection device 7 comprises a carrier plate 701 and a plurality of activated carbon flow channels 702 connected to the bottom surface of the carrier plate 701. Gaps are left among the activated carbon flow channels 702, and the gaps are SRG gas flow channels 703. The top and bottom of the activated carbon flow channels 702 are open structures. The top of the SRG gas flow channel 703 is the carrier plate 701, and the bottom thereof is an open structure.
Preferably, the top of the adsorption tower 8 is provided with a first level gauge 11. The second level indicator 12 is arranged at the first feeding hole A01 of the desorption tower A. The second feeding port A02 of the desorption tower A is provided with a third level indicator 13.
Preferably, the lower portion of the second blanking valve 10 is provided with a vibrating screen 14.
According to a second embodiment of the present invention, there is provided a method of purifying flue gas:
a method of cleaning flue gas using the above flue gas cleaning system, the method comprising the steps of:
1) the raw flue gas is conveyed into the adsorption tower 8 through a flue gas inlet of the activated carbon adsorption tower 8, the activated carbon adsorption of the adsorption tower 8 treats the raw flue gas, and pollutants in the raw flue gas are adsorbed by the activated carbon in the adsorption tower 8; the treated flue gas is discharged from a flue gas outlet of the adsorption tower 8;
2) the active carbon adsorbed with the pollutants in the adsorption tower 8 is discharged through a first baiting valve 9 at the bottom of the adsorption tower 8, and then is conveyed to a first feed inlet A01 of the desorption tower A through a first conveying device D1, and the active carbon adsorbed with the pollutants is heated and regenerated in the desorption tower A and is discharged through a second baiting valve 10 at the bottom of the desorption tower A;
3) the active carbon discharged from the desorption tower A is divided into two parts; one part of the flue gas is conveyed to an activated carbon inlet of the adsorption tower 8 through a second conveying device D2, and the raw flue gas is circularly adsorbed and treated; the other part is conveyed to a second feeding hole A02 of the desorption tower A through a third conveying device D3 and then enters an SRG gas dust removal device 4, the activated carbon is used for removing dust in the SRG gas, and the SRG gas collected by the SRG gas collecting device 7 is dedusted by the SRG gas dust removal device 4 and then is discharged from an SRG gas outlet 201.
Preferably, step 2) further comprises: the activated carbon discharged from the desorption tower a is screened by the vibrating screen 14, and then dust particles in the activated carbon are removed, and then the activated carbon is conveyed to the activated carbon inlet of the adsorption tower 8 by the second conveying device D2 and is conveyed to the second feed inlet a02 of the desorption tower a by the third conveying device D3.
In the present invention, the method further comprises: and 4) supplementing new active carbon from a second feeding hole A02 of the desorption tower A through a supplement conveying pipeline L to enter the desorption tower A according to the amount of the active carbon required by the treatment of the raw flue gas in the adsorption tower 8, the treatment amount of the desorption active carbon in the desorption tower A and the amount of the active carbon dust removed by screening through the vibrating screen 14.
In the invention, the step 4) is specifically as follows:
a) detecting the raw flue gas entering the adsorption tower 8, calculating the amount of the active carbon required by the raw flue gas in the adsorption tower 8 by combining the pollutant removal efficiency requirement, and obtaining the blanking amount M of the adsorption tower 81；
b) According to the relationship between the frequency of the first blanking valve 9 and the blanking amount of the adsorption tower 8, adjusting the frequency of the first blanking valve 9 to be equal to the blanking amount M of the adsorption tower 81Corresponding frequency f1；
c) A target level L of the second level gauge 12 below the first inlet A01 of the analysis column A was setObject 2Reading the level L of the second level indicator 122According to L2And LObject 2The frequency f of the second blanking valve 10 is adjusted2So that L is2＝LObject 2；
d) According to the relationship between the frequency of the second blanking valve 10 and the blanking amount of the analysis tower A, the blanking amount of the analysis tower A and the frequency f of the second blanking valve 10 are obtained2Corresponding blanking amount M2；
e) Determining the flow M of the screened outer-discharge activated carbon of the vibrating screen 14 below the desorption tower AOuter dischargeAccordingly, the total flow rate M of the activated carbon conveyed by the second conveying device D2 and the third conveying device D32'＝M2-MOuter discharge(ii) a The amount of the feed of the second transfer device D2 to the adsorption tower 8 was kept at M1Then, the third conveyer D2 feeds the second feed opening A02 of the desorption tower A with the amount M3＝M2'-M1；
f) A target level L of the third level gauge 13 below the second inlet A02 of the analysis column A was setTarget 3Reading the level L of the third level indicator 133When L is present3＜LTarget 3In the process, new active carbon is supplemented to a second feed inlet A02 of the desorption tower A through a supplement material conveying pipeline L; when L is3＞LTarget 3When the reaction is finished, stopping supplementing new active carbon into the desorption tower A; finally, the product is processedSo that L3＝LTarget 3。
In the invention, the raw flue gas entering the adsorption tower 8 is detected in the step a), the amount of the activated carbon required by the raw flue gas treated in the adsorption tower 8 is calculated, and the feeding amount M of the adsorption tower 8 is obtained1The method specifically comprises the following steps:
calculating SO to be processed by the adsorption tower 82Amount of NOx: detecting the flow of the original flue gas as Q and the concentration of sulfur dioxide in the original flue gas as
Figure BDA0001934123570000137
The concentration of nitrogen oxides in the raw flue gas is CNOxThus, the adsorption tower 8 is required to treat SO2The amounts of NOx are:
Figure BDA0001934123570000131
WNOx＝ηNOx×Q×CNOx/106；………(2)
in the formula (1), the reaction mixture is,
Figure BDA0001934123570000138
SO to be treated for the adsorption column 82The amount of (2) is unit kg/h; q is the flow of the original flue gas in Nm3/h；
Figure BDA00019341235700001310
Is SO in the original flue gas2Concentration of (2) in mg/Nm3；
Figure BDA0001934123570000134
Is SO2The removal efficiency of (2); in the formula (2), WNOxThe amount of NOx to be treated by the adsorption tower 8 is unit kg/h; cNOxThe concentration of nitrogen oxide in the original smoke is unit mg/Nm3；ηNOxEfficiency of NOx removal;
based on
Figure BDA0001934123570000139
And WNOxCalculating the feed amount M of the adsorption tower 81：
Figure BDA0001934123570000136
In formula (3), M1The unit kg/h is the blanking amount of the adsorption tower 8; k is a radical of1Is the first coefficient, k1A value of 5 to 50, preferably 8 to 40, more preferably 10 to 20; k is a radical of2Is the second coefficient, k2Values of 1 to 40, preferably 3 to 30, more preferably 5 to 20.
In the invention, the frequency f of the first blanking valve (9) in step b) is1The amount of the feed M to the adsorption tower (8)1The relationship (c) is specifically as follows: m1＝f1×k4×l1×d1 room×ρ1/r1×d1 straightWherein: k is a radical of4Fourth coefficient, l1Is the length of the first blanking valve round roller, d1 roomIs the gap of the first blanking valve round roller, rho1Is the bulk density of activated carbon in the adsorption tower, r1Maximum rotational speed of the first discharge valve round roll, d1 straightThe diameter of the first blanking valve round roller; k is a radical of4The value is 0.01 to 0.2, preferably 0.03 to 0.15, more preferably 0.05 to 0.1.
In the invention, the frequency f of the second discharge valve (10) in step d) is2The amount of feed M to the analytical column (A)2The relationship (c) is specifically as follows: m2＝f2×k5×l2×d2 room×ρ2/r2×d2 straightWherein: k is a radical of5Fifth coefficient, l2Length of the second discharge valve round roll, d2 roomIs the gap of the second blanking valve round roller, rho2To resolve the bulk density of the activated carbon in the column, r2Maximum rotational speed of the second discharge valve round roll, d2 straightThe diameter of the second blanking valve round roller; k is a radical of5The value is 0.01 to 0.2, preferably 0.03 to 0.15, more preferably 0.05 to 0.1.
In the present invention, the frequency f of the second baiting valve 10 is adjusted in the step c)2The method specifically comprises the following steps:
when L is2＞LObject 2While increasing the frequency f of the second baiting valve 102(ii) a When L is2＜LObject 2While reducing the frequency f of the second baiting valve 102Finally make L2＝LObject 2。
In the invention, the flow M of the externally discharged activated carbon of the desorption tower A is determined in the step e)Outer dischargeThe method specifically comprises the following steps:
Mouter discharge＝k3×M2；………(4)
And satisfies the following conditions: d2/(d1+d2)＞k3；………(5)
In the formula (4), k3The third coefficient is the value range of 1-3%; m2The unit kg/h is the blanking amount of the analysis tower A; in the formula (5), d1The width between the inner wall of the desorption tower A and the first partition plate 5 is close to one side right below the first feeding hole A01; d2The width of the SRG gas dust removing device 4, i.e., the width between the second partition 6 and the SRG gas outlet 201 on the side immediately below the second feed opening a 02.
Example 1
As shown in fig. 3 and 4, the flue gas purification system comprises a desorption tower a, an adsorption tower 8, a first conveying device D1, a second conveying device D2 and a third conveying device D3. The desorption tower A comprises a heating section 1, a transition section 2 and a cooling section 3. The heating section 1 is arranged at the upper part of the analysis tower A, the cooling section 3 is arranged at the lower part of the analysis tower A, and the transition section 2 is arranged between the heating section 1 and the cooling section 3. The side wall of the transition section 2 is provided with an SRG gas outlet 201. The top of the desorption tower A is provided with a first feed inlet A01 and a second feed inlet A02. And an SRG gas dust removal device 4 is arranged in the transition section 2 and is positioned right below the second feeding hole A02. The SRG gas dust removal device 4 is located at the inner side of the SRG gas outlet 201, and the SRG gas dust removal device 4 and the SRG gas outlet 201 are tightly arranged. The first conveying device D1 is connected with the activated carbon outlet of the adsorption tower 8 and the first feed inlet A01 of the desorption tower A, the second conveying device D2 is connected with the activated carbon outlet of the desorption tower A and the activated carbon inlet of the adsorption tower 8, and the third conveying device D3 is connected with the activated carbon outlet of the desorption tower A and the second feed inlet A02 of the desorption tower A. The bottom of the adsorption tower 8 is provided with a first blanking valve 9. The bottom of the desorption tower A is provided with a second blanking valve 10. The second feed inlet a02 of the stripper column a is also connected to a make-up feed conveying line L.
A first partition plate 5 is arranged between the first feed opening A01 and the second feed opening A02. The lower end of the first partition plate 5 is connected with the top of the heating section 1. A second partition plate 6 is arranged on one side of the top of the SRG gas dust removal device 4, and the second partition plate 6 is arranged on the side opposite to the SRG gas outlet 201. The upper end of the second clapboard 6 is connected with the bottom of the heating section 1, and the lower end is connected with the SRG gas dust removal device 4. The first partition plate 5 and the second partition plate 6 are both arranged in parallel with the side where the SRG gas outlet 201 is located, and the second partition plate 6 is arranged right below the first partition plate 5.
And the SRG gas dust removal device 4 is an activated carbon channel layer. The top and the bottom of the active carbon channel layer are both of an open structure. The left side and the right side of the SRG gas dust removal device 4 are respectively of a shutter structure.
An SRG gas collecting device 7 is arranged in the transition section 2. The SRG gas dust removal device 4 is arranged between the SRG gas collecting device 7 and the SRG gas outlet 201. The SRG gas collection assembly 7 includes a carrier plate 701 and a plurality of activated carbon flow channels 702 connected to the bottom surface of the carrier plate 701. Gaps are left among the activated carbon flow channels 702, and the gaps are SRG gas flow channels 703. The top and bottom of the activated carbon flow channels 702 are open structures. The top of the SRG gas flow channel 703 is the carrier plate 701, and the bottom thereof is an open structure.
The top of the adsorption tower 8 is provided with a first level indicator 11. The second level indicator 12 is arranged at the first feeding hole A01 of the desorption tower A. The second feeding port A02 of the desorption tower A is provided with a third level indicator 13. The lower portion of the second blanking valve 10 is provided with a vibrating screen 14.
Example 2
A method for purifying flue gas using the flue gas purification system of embodiment 1, comprising the steps of:
1) the raw flue gas is conveyed into the adsorption tower 8 through a flue gas inlet of the activated carbon adsorption tower 8, the activated carbon adsorption of the adsorption tower 8 treats the raw flue gas, and pollutants in the raw flue gas are adsorbed by the activated carbon in the adsorption tower 8; the treated flue gas is discharged from a flue gas outlet of the adsorption tower 8;
2) the active carbon adsorbed with the pollutants in the adsorption tower 8 is discharged through a first baiting valve 9 at the bottom of the adsorption tower 8, and then is conveyed to a first feed inlet A01 of the desorption tower A through a first conveying device D1, and the active carbon adsorbed with the pollutants is heated and regenerated in the desorption tower A and is discharged through a second baiting valve 10 at the bottom of the desorption tower A;
3) the active carbon discharged from the desorption tower A is divided into two parts; one part of the flue gas is conveyed to an activated carbon inlet of the adsorption tower 8 through a second conveying device D2, and the raw flue gas is circularly adsorbed and treated; the other part is conveyed to a second feeding hole A02 of the desorption tower A through a third conveying device D3 and then enters an SRG gas dust removal device 4, the activated carbon is used for removing dust in the SRG gas, and the SRG gas collected by the SRG gas collecting device 7 is dedusted by the SRG gas dust removal device 4 and then is discharged from an SRG gas outlet 201.
Example 3
Example 2 is repeated except that step 2) further comprises: the activated carbon discharged from the desorption tower a is screened by the vibrating screen 14, and then dust particles in the activated carbon are removed, and then the activated carbon is conveyed to the activated carbon inlet of the adsorption tower 8 by the second conveying device D2 and is conveyed to the second feed inlet a02 of the desorption tower a by the third conveying device D3.
Example 4
Example 3 is repeated except that the method further comprises: and 4) supplementing new active carbon from a second feeding hole A02 of the desorption tower A through a supplement conveying pipeline L to enter the desorption tower A according to the amount of the active carbon required by the treatment of the raw flue gas in the adsorption tower 8, the treatment amount of the desorption active carbon in the desorption tower A and the amount of the active carbon dust removed by screening through the vibrating screen 14.
The step 4) is specifically as follows:
a) detecting the raw flue gas entering the adsorption tower 8, calculating the amount of the active carbon required by the raw flue gas in the adsorption tower 8 by combining the pollutant removal efficiency requirement, and obtaining the blanking amount M of the adsorption tower 81：
Calculating SO to be processed by the adsorption tower 82Amount of NOx: detecting the flow of the original smoke as Q106Nm3/h、The concentration of sulfur dioxide in the original flue gas is
Figure BDA0001934123570000165
The concentration of nitrogen oxides in the raw flue gas is CNOx＝CNOx＝300mg/Nm3，SO2NOx removal efficiencies of 95% and 85%, respectively, whereby the adsorption tower 8 treats the SO2The amounts of NOx are:
Figure BDA0001934123570000161
WNOx＝ηNOx×Q×CNOx/106＝255；………(2)
in the formula (1), the reaction mixture is,
Figure BDA0001934123570000162
SO to be treated for the adsorption column 82The amount of (2) is unit kg/h; q is the flow of the original flue gas in Nm3/h；
Figure BDA0001934123570000166
Is SO in the original flue gas2Concentration of (2) in mg/Nm3；
Figure BDA0001934123570000164
Is SO2The removal efficiency of (2); in the formula (2), WNOxThe amount of NOx to be treated by the adsorption tower 8 is unit kg/h; cNOxThe concentration of nitrogen oxide in the original smoke is unit mg/Nm3；ηNOxEfficiency of NOx removal;
based on
Figure BDA0001934123570000167
And WNOxCalculating the feed amount M of the adsorption tower 81：
Figure BDA0001934123570000168
In formula (3), M1The unit kg/h is the blanking amount of the adsorption tower 8; k is a radical of1Is a first coefficient, value 15; k is a radical of2Is the second coefficient, and has a value of 16.
b) According to the relationship between the frequency of the first blanking valve 9 and the blanking amount of the adsorption tower 8, adjusting the frequency of the first blanking valve 9 to be equal to the blanking amount M of the adsorption tower 81Corresponding frequency f1。
c) A target level L of the second level gauge 12 below the first inlet A01 of the analysis column A was setObject 2At 3m, the level L of the second level indicator 12 is read2Is 3m, according to L2And LObject 2The frequency f of the second blanking valve 10 is adjusted2So that L is2＝LObject 2：
When L is2＞LObject 2While increasing the frequency f of the second baiting valve 102(ii) a When L is2＜LObject 2While reducing the frequency f of the second baiting valve 102Finally make L2＝LObject 2。
d) According to the relationship between the frequency of the second blanking valve 10 and the blanking amount of the analysis tower A, the blanking amount of the analysis tower A and the frequency f of the second blanking valve 10 are obtained2Corresponding blanking amount M2。
e) Determining the flow M of the screened outer-discharge activated carbon of the vibrating screen 14 below the desorption tower AOuter discharge：
MOuter discharge＝k3×M2；………(4)
And satisfies the following conditions: d2/(d1+d2)＞k3；………(5)
In the formula (4), k3Is a third coefficient, the value is 1.5%; m2The unit kg/h is the blanking amount of the analysis tower A; in the formula (5), d1The width between the inner wall of the desorption tower A and the first partition plate 5 is close to one side right below the first feeding hole A01; d2The width of the SRG gas dust removing device 4, i.e. the width between the second partition plate 6 and the SRG gas outlet 201 on the side close to the right below the second feed opening a 02;
thereby, the total flow of the activated carbon conveyed by the second conveying device D2 and the third conveying device D3Quantity M2'＝M2-MOuter discharge(ii) a The amount of the feed of the second transfer device D2 to the adsorption tower 8 was kept at M1Then, the third conveyer D2 feeds the second feed opening A02 of the desorption tower A with the amount M3＝M2'-M1。
f) A target level L of the third level gauge 13 below the second inlet A02 of the analysis column A was setTarget 3At 3m, the level L of the third level indicator 13 is read3Is 3m, when L3＜LTarget 3In the process, new active carbon is supplemented to a second feed inlet A02 of the desorption tower A through a supplement material conveying pipeline L; when L is3＞LTarget 3When the reaction is finished, stopping supplementing new active carbon into the desorption tower A; finally make L3＝LTarget 3。
Application example 1
The activated carbon desorption tower provided by the embodiment 1 of the application is adopted to carry out desorption activation (or regeneration) treatment on the activated carbon containing pollutants, and 600m of the activated carbon is treated2The flue gas generated by the sintering machine passes through activated carbon adsorption tower to be treated, the activated carbon containing pollutants is discharged from an SRG gas outlet of an desorption tower, and the dust content is lower than 0.5g/m3。
Application example 2
Adopting an activated carbon desorption tower with the application number of CN201720876280 to carry out desorption activation (or regeneration) treatment on the activated carbon containing the pollutants, and treating the activated carbon with the treatment depth of 600m2The flue gas generated by the sintering machine passes through activated carbon adsorption tower to be treated, the activated carbon containing pollutants is discharged from an SRG gas outlet of an analytical tower, and the dust content is 1.5g/m3。

Claims (27)

1. A flue gas purification system comprises a desorption tower (A), an adsorption tower (8), a first conveying device (D1), a second conveying device (D2) and a third conveying device (D3); the desorption tower (A) comprises a heating section (1), a transition section (2) and a cooling section (3); the heating section (1) is arranged at the upper part of the analysis tower (A), the cooling section (3) is arranged at the lower part of the analysis tower (A), and the transition section (2) is arranged between the heating section (1) and the cooling section (3); the side wall of the transition section (2) is provided with an SRG gas outlet (201); the top of the desorption tower (A) is provided with a first feed inlet (A01) and a second feed inlet (A02); an SRG gas dust removal device (4) is arranged in the transition section (2) and is positioned right below the second feeding hole (A02); the SRG gas dust removal device (4) is positioned on the inner side of the SRG gas outlet (201), and the SRG gas dust removal device (4) and the SRG gas outlet (201) are tightly arranged; the first conveying device (D1) is connected with the activated carbon outlet of the adsorption tower (8) and the first feeding hole (A01) of the desorption tower (A), the second conveying device (D2) is connected with the activated carbon outlet of the desorption tower (A) and the activated carbon inlet of the adsorption tower (8), and the third conveying device (D3) is connected with the activated carbon outlet of the desorption tower (A) and the second feeding hole (A02) of the desorption tower (A); a first blanking valve (9) is arranged at the bottom of the adsorption tower (8); the bottom of the desorption tower (A) is provided with a second blanking valve (10); the second feed inlet (A02) of the stripping tower (A) is also connected with a replenisher conveying pipeline (L).
2. The flue gas purification system according to claim 1, wherein: a first partition plate (5) is arranged between the first feed opening (A01) and the second feed opening (A02); the lower end of the first clapboard (5) is connected with the top of the heating section (1); and/or
A second partition plate (6) is arranged on one side of the top of the SRG gas dust removal device (4), and the second partition plate (6) is arranged on the side opposite to the SRG gas outlet (201); the upper end of the second clapboard (6) is connected with the bottom of the heating section (1) and the lower end is connected with the SRG gas dust removal device (4).
3. The flue gas purification system according to claim 2, wherein: the first partition plate (5) and the second partition plate (6) are arranged in parallel with the side face where the SRG gas outlet (201) is located, and the second partition plate (6) is arranged under the first partition plate (5).
4. A flue gas cleaning system according to any one of claims 1-3, characterized in that: the SRG gas dust removal device (4) is an activated carbon channel layer; the top and the bottom of the active carbon channel layer are both of an open structure.
5. The flue gas purification system according to claim 4, wherein: the left side and the right side of the SRG gas dust removal device (4) are respectively of a shutter structure or a porous plate structure.
6. The flue gas purification system according to any one of claims 1-3, 5, wherein: an SRG gas collecting device (7) is arranged in the transition section (2); the SRG gas dust removal device (4) is arranged between the SRG gas collecting device (7) and the SRG gas outlet (201).
7. The flue gas purification system according to claim 6, wherein: the SRG gas collecting device (7) comprises a bearing plate (701) and a plurality of activated carbon circulation channels (702) connected to the bottom surface of the bearing plate (701); gaps are reserved among the activated carbon flow channels (702), and the gaps are SRG gas flow channels (703); the top and the bottom of the activated carbon flow channel (702) are both open structures; the top of the SRG gas flow channel (703) is a carrier plate (701), and the bottom is an open structure.
8. The flue gas purification system according to any one of claims 1-3, 5, 7, wherein: a first level indicator (11) is arranged at the top of the adsorption tower (8); a second level indicator (12) is arranged at the first feed inlet (A01) of the desorption tower (A); a third level indicator (13) is arranged at the second feeding hole (A02) of the desorption tower (A).
9. The flue gas purification system according to claim 4, wherein: a first level indicator (11) is arranged at the top of the adsorption tower (8); a second level indicator (12) is arranged at the first feed inlet (A01) of the desorption tower (A); a third level indicator (13) is arranged at the second feeding hole (A02) of the desorption tower (A).
10. The flue gas purification system according to claim 6, wherein: a first level indicator (11) is arranged at the top of the adsorption tower (8); a second level indicator (12) is arranged at the first feed inlet (A01) of the desorption tower (A); a third level indicator (13) is arranged at the second feeding hole (A02) of the desorption tower (A).
11. The flue gas purification system according to claim 8, wherein: the lower part of the second blanking valve (10) is provided with a vibrating screen (14).
12. The flue gas purification system according to claim 9 or 10, wherein: the lower part of the second blanking valve (10) is provided with a vibrating screen (14).
13. A flue gas cleaning method using the flue gas cleaning system according to any one of claims 1 to 12, the method comprising the steps of:
1) the raw flue gas is conveyed into the adsorption tower (8) through a flue gas inlet of the activated carbon adsorption tower (8), the activated carbon adsorption of the adsorption tower (8) treats the raw flue gas, and pollutants in the raw flue gas are adsorbed by the activated carbon in the adsorption tower (8); the treated flue gas is discharged from a flue gas outlet of the adsorption tower (8);
2) the active carbon adsorbed with the pollutants in the adsorption tower (8) is discharged through a first blanking valve (9) at the bottom of the adsorption tower (8), then is conveyed to a first feeding hole (A01) of the desorption tower (A) through a first conveying device (D1), is heated and regenerated in the desorption tower (A), and is discharged through a second blanking valve (10) at the bottom of the desorption tower (A);
3) the activated carbon discharged from the desorption tower (A) is divided into two parts; one part of the flue gas is conveyed to an activated carbon inlet of the adsorption tower (8) through a second conveying device (D2) to circularly adsorb and treat the raw flue gas; and the other part is conveyed to a second feeding hole (A02) of the desorption tower (A) through a third conveying device (D3) and then enters an SRG gas dust removal device (4), the part of activated carbon is used for removing dust in the SRG gas, and the SRG gas collected by the SRG gas collecting device (7) is discharged from an SRG gas outlet (201) after being subjected to dust removal by the SRG gas dust removal device (4).
14. The flue gas purification method according to claim 13, wherein: step 2) also includes: the activated carbon discharged from the desorption tower (A) is screened by a vibrating screen (14), dust particles in the activated carbon are removed, and then the activated carbon is conveyed to an activated carbon inlet of the adsorption tower (8) through a second conveying device (D2) and is conveyed to a second feeding hole (A02) of the desorption tower (A) through a third conveying device (D3).
15. The flue gas purification method according to claim 14, wherein: the method further comprises the following steps: and 4) supplementing new active carbon from a second feeding hole (A02) of the desorption tower (A) into the desorption tower (A) through a supplementing material conveying pipeline (L) according to the amount of the active carbon required by the treatment of the raw flue gas in the adsorption tower (8), the treatment amount of the desorption active carbon in the desorption tower (A) and the amount of the active carbon dust removed by screening through a vibrating screen (14).
16. The flue gas purification method according to claim 15, wherein: the step 4) is specifically as follows:
a) detecting the raw flue gas entering the adsorption tower (8), and calculating the amount of the activated carbon required by the raw flue gas treated in the adsorption tower (8) by combining the pollutant removal efficiency requirement to obtain the feed amount M of the adsorption tower (8)1；
b) According to the relation between the frequency of the first blanking valve (9) and the blanking amount of the adsorption tower (8), the frequency of the first blanking valve (9) is adjusted to be equal to the blanking amount M of the adsorption tower (8)1Corresponding frequency f1；
c) A target level L of a second level gauge (12) below a first feed opening (A01) of an analytical column (A) is setObject 2Reading the level L of the second level indicator (12)2According to L2And LObject 2In the magnitude relation of (a), adjusting the frequency f of the second discharge valve (10)2So that L is2＝LObject 2；
d) According to the relation between the frequency of the second blanking valve (10) and the blanking amount of the analysis tower (A), the blanking amount of the analysis tower (A) and the frequency f of the second blanking valve (10) are obtained2Corresponding blanking amount M2；
e) Determining the flow M of the screened outer-discharge activated carbon of the vibrating screen (14) below the desorption tower (A)Outer dischargeThereby, the total flow rate M of the activated carbon conveyed by the second conveying device (D2) and the third conveying device (D3)2'＝M2-MOuter discharge(ii) a Maintaining the feeding amount of the second conveying device (D2) to the adsorption tower (8) at M1A second feeding of the desorption column (A) by the third transport device (D2)The feeding amount M of the port (A02)3＝M2'-M1；
f) A target level L of a third level gauge (13) below a second feed opening (A02) of the analysis column (A) is setTarget 3Reading the level L of the third level indicator (13)3When L is present3＜LTarget 3In the process, the second feed inlet (A02) of the desorption tower (A) is supplemented with new active carbon through a supplement material conveying pipeline (L); when L is3＞LTarget 3Stopping supplementing new active carbon to the desorption tower (A); finally make L3＝LTarget 3。
17. The flue gas purification method according to claim 16, wherein: in the step a), the raw flue gas entering the adsorption tower (8) is detected, the amount of the activated carbon required by the raw flue gas treated in the adsorption tower (8) is calculated, and the feeding amount M of the adsorption tower (8) is obtained1The method specifically comprises the following steps:
calculating SO to be processed by the adsorption tower (8)2Amount of NOx: detecting the flow of the original flue gas as Q and the concentration of sulfur dioxide in the original flue gas as
Figure RE-FDA0003120372580000041
The concentration of nitrogen oxides in the raw flue gas is CNOxThus, the adsorption tower (8) is required to treat SO2The amounts of NOx are:
Figure RE-FDA0003120372580000042
WNOx＝ηNOx×Q×CNOx/106；………(2)
in the formula (1), the reaction mixture is,
Figure RE-FDA0003120372580000043
SO to be treated for the adsorption column (8)2The amount of (2) is unit kg/h; q is the flow of the original flue gas in Nm3/h；
Figure RE-FDA0003120372580000044
Is SO in the original flue gas2Concentration of (2) in mg/Nm3；
Figure RE-FDA0003120372580000045
Is SO2The removal efficiency of (2); in the formula (2), WNOxThe amount of NOx to be treated by the adsorption tower (8) is unit kg/h; cNOxThe concentration of nitrogen oxide in the original smoke is unit mg/Nm3；ηNOxEfficiency of NOx removal;
based on
Figure RE-FDA0003120372580000046
And WNOxCalculating the blanking amount M of the adsorption tower (8)1：
Figure RE-FDA0003120372580000047
In formula (3), M1The unit kg/h is the blanking amount of the adsorption tower (8); k is a radical of1Is the first coefficient, k1A value of 5-50; k is a radical of2Is the second coefficient, k2The value is 1-40.
18. The flue gas purification method according to claim 17, wherein: k is a radical of1The value is 8-40; k is a radical of2The value is 3-30.
19. The flue gas purification method according to claim 18, wherein: k is a radical of1A value of 10-20; k is a radical of2The value is 5-20.
20. The flue gas purification method according to any one of claims 16 to 19, wherein: frequency f of the first blanking valve (9) in step b)1The amount of the feed M to the adsorption tower (8)1The relationship (c) is specifically as follows: m1＝f1×k4×l1×d1 room×ρ1/r1×d1 straightWherein: k is a radical of4Fourth step ofCoefficient of l1Is the length of the first blanking valve round roller, d1 roomIs the gap of the first blanking valve round roller, rho1Is the bulk density of activated carbon in the adsorption tower, r1Maximum rotational speed of the first discharge valve round roll, d1 straightThe diameter of the first blanking valve round roller; k is a radical of4The value is 0.01-0.2; and/or
Frequency f of the second discharge valve (10) in step d)2The amount of feed M to the analytical column (A)2The relationship (c) is specifically as follows: m2＝f2×k5×l2×d2 room×ρ2/r2×d2 straightWherein: k is a radical of5Fifth coefficient, l2Length of the second discharge valve round roll, d2 roomIs the gap of the second blanking valve round roller, rho2To resolve the bulk density of the activated carbon in the column, r2Maximum rotational speed of the second discharge valve round roll, d2 straightThe diameter of the second blanking valve round roller; k is a radical of5The value is 0.01-0.2.
21. The flue gas purification method according to claim 20, wherein: k is a radical of4The value is 0.03-0.15; and/or
k5The value is 0.03-0.15.
22. The flue gas purification method according to claim 21, wherein: k is a radical of4A value of 0.05-0.1; and/or
k5The value is 0.05-0.1.
23. A flue gas purification method according to any one of claims 16-19, 21-22, characterized in that: said adjusting of the frequency f of the second discharge valve (10) in step c)2The method specifically comprises the following steps:
when L is2＞LObject 2While increasing the frequency f of the second discharge valve (10)2(ii) a When L is2＜LObject 2While reducing the frequency f of the second discharge valve (10)2Finally make L2＝LObject 2。
24. The flue gas purification method according to claim 20, wherein: said adjusting of the frequency f of the second discharge valve (10) in step c)2The method specifically comprises the following steps:
when L is2＞LObject 2While increasing the frequency f of the second discharge valve (10)2(ii) a When L is2＜LObject 2While reducing the frequency f of the second discharge valve (10)2Finally make L2＝LObject 2。
25. A method for flue gas purification according to any of claims 16-19, 21-22, 24, characterized in that: determining the flow M of the externally discharged activated carbon of the desorption tower (A) in the step e)Outer dischargeThe method specifically comprises the following steps:
Mouter discharge＝k3×M2；………(4)
And satisfies the following conditions: d2/(d1+d2)＞k3；………(5)
In the formula (4), k3The third coefficient is the value range of 1-3%; m2The feed amount of the resolving tower (A) is unit kg/h; in the formula (5), d1The width between the inner wall of the desorption tower (A) and the first partition plate (5) is close to one side right below the first feeding hole (A01); d2The width of the SRG gas dust removal device (4), namely the width between the second partition plate (6) and the SRG gas outlet (201) close to the side right below the second feed port (A02).
26. The flue gas purification method according to claim 20, wherein: determining the flow M of the externally discharged activated carbon of the desorption tower (A) in the step e)Outer dischargeThe method specifically comprises the following steps:
Mouter discharge＝k3×M2；………(4)
And satisfies the following conditions: d2/(d1+d2)＞k3；………(5)
In the formula (4), k3The third coefficient is the value range of 1-3%; m2The feed amount of the resolving tower (A) is unit kg/h; in the formula (5), d1Is near the first feed opening (A0)1) The width between the inner wall of the desorption tower (A) and the first clapboard (5) at one side right below the desorption tower (A); d2The width of the SRG gas dust removal device (4), namely the width between the second partition plate (6) and the SRG gas outlet (201) close to the side right below the second feed port (A02).
27. The flue gas purification method according to claim 23, wherein: determining the flow M of the externally discharged activated carbon of the desorption tower (A) in the step e)Outer dischargeThe method specifically comprises the following steps:
Mouter discharge＝k3×M2；………(4)
And satisfies the following conditions: d2/(d1+d2)＞k3；………(5)
In the formula (4), k3The third coefficient is the value range of 1-3%; m2The feed amount of the resolving tower (A) is unit kg/h; in the formula (5), d1The width between the inner wall of the desorption tower (A) and the first partition plate (5) is close to one side right below the first feeding hole (A01); d2The width of the SRG gas dust removal device (4), namely the width between the second partition plate (6) and the SRG gas outlet (201) close to the side right below the second feed port (A02).
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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN207342440U (en) * 2017-07-19 2018-05-11 中冶长天国际工程有限责任公司 A kind of Analytic Tower
CN108479344A (en) * 2018-04-08 2018-09-04 中冶长天国际工程有限责任公司 A kind of desulphurization denitration removes ammonia system
CN108525464A (en) * 2018-06-06 2018-09-14 中冶长天国际工程有限责任公司 A kind of level control method and device for system for desulfuration and denitration
CN108619850A (en) * 2018-04-08 2018-10-09 中冶长天国际工程有限责任公司 The recycle device of powdered carbon

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8197581B2 (en) * 2007-04-23 2012-06-12 ESC Enviroenergy, LLC Self-regulating bio-gas treatment system
CA2996008C (en) * 2015-09-25 2019-09-17 Exxonmobil Research And Engineering Company Cyclic thermal swing adsorption with direct heat transfer using a heat transfer fluid

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN207342440U (en) * 2017-07-19 2018-05-11 中冶长天国际工程有限责任公司 A kind of Analytic Tower
CN108479344A (en) * 2018-04-08 2018-09-04 中冶长天国际工程有限责任公司 A kind of desulphurization denitration removes ammonia system
CN108619850A (en) * 2018-04-08 2018-10-09 中冶长天国际工程有限责任公司 The recycle device of powdered carbon
CN108525464A (en) * 2018-06-06 2018-09-14 中冶长天国际工程有限责任公司 A kind of level control method and device for system for desulfuration and denitration

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