CN111617595A - Method for starting active coke dry adsorption purification device - Google Patents
Method for starting active coke dry adsorption purification device Download PDFInfo
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- CN111617595A CN111617595A CN201910152920.8A CN201910152920A CN111617595A CN 111617595 A CN111617595 A CN 111617595A CN 201910152920 A CN201910152920 A CN 201910152920A CN 111617595 A CN111617595 A CN 111617595A
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- 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
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Abstract
The invention relates to a startup method of an active coke dry adsorption purification device, which comprises the following steps: (1) introducing air into an active coke adsorption tower filled with fresh active coke to passivate the fresh active coke; (2) introducing nitrogen into the activated coke adsorption column to displace at least a portion of the air; (3) introducing the flue gas to be purified into the active coke adsorption tower, wherein the initial introduction amount of the flue gas to be purified does not exceed 80% of the design load of the device, gradually increasing the introduction amount of the flue gas to be purified until the design load of the device reaches 100%, and normally operating the active coke dry-method adsorption purification device. According to the start-up method, before the flue gas is introduced, the air circulation is adopted to passivate the active coke, so that the adsorption activity of the active coke is reduced, the overtemperature phenomenon of an active coke bed layer when the flue gas is introduced is avoided, the air passivation process of the active coke can be carried out in advance independently of an upstream system, the start-up time of the device is shortened, and the safe and stable operation of the active coke adsorption tower is ensured.
Description
Technical Field
The disclosure relates to the field of flue gas desulfurization process by an active coke dry method, in particular to a start-up method of an active coke dry method adsorption purification device.
Background
The active coke dry purification technology starts to be industrially applied in the 80 th of the 20 th century, and has the outstanding advantages of high desulfurization efficiency, no water consumption in reaction, no waste water and residue discharge, no equipment corrosion problem and the like. With the increasing environmental protection requirement, the technology draws more and more attention and is increasingly widely applied. The active coke-drying purification technology is applied to the catalytic cracking device, SO that SO in the regenerated flue gas can be effectively removed2/SO3Simultaneously to NOxParticulate matter and VOCs etc. also have the effect of desorption in coordination, combine upstream SCR and low reaches sack cleaner, whole clean system can purify regeneration flue gas to satisfying the standard requirement.
The active coke adsorption desulfurization is mainly based on chemical adsorption, and the process is a strong exothermic reaction. The reaction heat released in normal operation is absorbed by the flue gas and the active coke, so that the temperature of the flue gas and the temperature of the bed layer are increased to a certain extent. Along with SO in the flue gas2The concentration is continuously increased, the heat emitted in the adsorption process is increased, the flue gas temperature and the bed layer temperature are continuously increased, and finally the active coke bed layer is possibly over-temperature or spontaneous combustion, SO that the SO in the flue gas treated by the existing active coke dry-method flue gas purification process2The concentration usually cannot exceed 5000mg/Nm3But in individual cases SO in flue gases2The concentration can reach 10000mg/Nm3. In addition, the higher the flue gas temperature is, the higher the oxidation exothermic temperature rise of the active coke adsorption bed layer is. Generally, the measure for controlling the temperature rise of the bed layer of the active coke adsorption tower is mainly to reduce SO in the flue gas to be purified2For treating high SO2Application of active coke dry purification process in gas concentrationAre significantly limited; and secondly, the temperature of the flue gas to be purified is reduced, and the heat release of the active coke bed layer due to oxidation is reduced so as to control the temperature rise of the bed layer.
The key equipment of the active coke dry purification technology is an active coke adsorption tower, a moving bed is usually adopted, the active coke loading is large, and the retention time in the tower is 5-7 days. When the existing active coke dry purification device is started for the first time, the amount of introduced flue gas is only 40-50% of the design load, the temperature of the flue gas is controlled to be not more than 120 ℃, the flue gas amount is gradually increased to the normal design load after the active coke adsorption tower runs for 7-8 days and the adsorption activity is correspondingly reduced, the whole starting process is long, usually for 7-10 days, and certain inconvenience is brought to the timely production of the device.
Disclosure of Invention
The invention aims to provide a startup method of an active coke dry-method adsorption purification device, which can safely and effectively control the flue gas temperature at the inlet of an active coke adsorption tower and the temperature rise of a bed layer of the adsorption tower, shorten the startup time and ensure the safe and stable operation of the active coke adsorption tower.
In order to achieve the above object, a first aspect of the present disclosure provides a method for operating an active coke dry adsorption purification apparatus, the method including the steps of:
(1) introducing air into an active coke adsorption tower filled with fresh active coke to passivate the fresh active coke;
(2) passing nitrogen into the activated coke adsorption column to displace at least a portion of the air;
(3) introducing the flue gas to be purified into the active coke adsorption tower, wherein the initial introduction amount of the flue gas to be purified is not more than 80% of the design load of the device, gradually increasing the introduction amount of the flue gas to be purified until the design load of the device is 100%, and normally operating the active coke dry method adsorption purification device.
Optionally, a clean flue gas circulation pipeline is connected between the adsorbed gas outlet of the active coke adsorption tower and the gas inlet to be adsorbed, and step (1) includes: and circulating the air in the active coke adsorption tower and the clean flue gas circulating pipeline, and gradually increasing the flow of the circulating air until the flow of the circulating air reaches 80-100% of the design load of the device, and then continuously circulating for 12-24 h.
Optionally, a mixed gas containing nitrogen and air is obtained at the gas outlet after adsorption of the active coke adsorption tower, and the step (2) comprises the following steps: and stopping introducing air, returning at least part of the mixed gas into the active coke adsorption tower, discharging the other part of the mixed gas to a chimney, and gradually increasing the flow of the mixed gas discharged to the chimney so as to perform the replacement.
Optionally, when the replacement in the step (2) is carried out for more than 2h and the oxygen content in the gas in the activated coke adsorption tower is not more than 5 vol%, the step (3) is carried out.
Optionally, step (3) comprises:
a first operation stage: stopping introducing nitrogen, wherein the introduction amount of the flue gas to be purified is 20-80% of the design load of the device; and dividing the flue gas discharged from the adsorbed gas outlet of the active coke adsorption tower into a first clean flue gas and a second clean flue gas, cooling the first clean flue gas by a flue gas cooler, returning the first clean flue gas to the active coke adsorption tower for clean flue gas circulation, and discharging the second clean flue gas to a chimney.
Optionally, an inlet air chamber and a plurality of active coke adsorption beds are sequentially arranged in the active coke adsorption tower along the flow direction of flue gas, and an interstage air chamber is arranged between every two adjacent active coke adsorption beds; the step (3) further comprises the following steps: returning the first clean flue gas to the inlet plenum and the interstage plenum, respectively.
Optionally, step (3) comprises: when the first operation stage is carried out for more than 12 hours and the temperature of the bed layer of the active coke adsorption tower is not more than 0.5 ℃ within 1 hour, carrying out a second operation stage;
the second operational phase comprises: the introduction of the flue gas to be purified is increased to 100% of the design load of the plant.
Optionally, when the second operation stage is performed for more than 6 hours, the total temperature rise of the flue gas passing through the active coke adsorption tower is not more than 15 ℃, and the temperature rise of the bed layer after stabilization is not more than 0.5 ℃ within 1 hour, the active coke dry method adsorption purification device can normally operate.
Optionally, the method further comprises: and (4) in the step (3), controlling the temperature of the flue gas to be purified not to be higher than the inlet flue gas temperature of the active coke adsorption tower during normal operation.
Optionally, the total start-up time of the method does not exceed 48 h.
By the technical scheme, the start-up method disclosed by the invention passivates the active coke by adopting air closed circulation on the fresh active coke when the active coke dry-method purification device is started for the first time, so that the adsorption activity of the active coke is reduced; meanwhile, after the system is switched into flue gas, the flue gas temperature at the inlet of the active coke adsorption tower and the temperature rise of the bed layer of the adsorption tower can be safely and effectively controlled, the start-up time is shortened, and the safe and stable operation of the active coke adsorption tower is ensured.
The start-up method has the advantages that:
(1) the activated coke is passivated by adopting air circulation before the flue gas is introduced into the activated coke adsorption tower, so that the adsorption activity of the activated coke is reduced, and the probability of over-temperature of an activated coke bed layer is greatly reduced when the flue gas is introduced;
(2) the start-up time is greatly shortened from the original 7-10 days to the current 2 days;
(3) by introducing air into the system, the air passivation process of the active coke can be performed in advance independently of an upstream system, and convenience is created for the start-up of the active coke dry-method purification device.
Additional features and advantages of the disclosure will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the disclosure and are incorporated in and constitute a part of this specification, illustrate embodiments of the disclosure and together with the description serve to explain the disclosure without limiting the disclosure. In the drawings:
fig. 1 is a process flow diagram of a specific embodiment of a method for operating an adsorption purification device by an active coke dry method according to the present disclosure.
Fig. 2 is a process flow diagram of another embodiment of the operation method of the active coke dry adsorption purification device of the present disclosure.
Description of the reference numerals
Device
A-dust remover B-active coke adsorption tower
B1-inlet air chamber B2-first stage adsorption bed layer
B3-interstage air chamber B4-second stage adsorption bed B5-outlet air chamber
C-clean flue gas induced draft fan D-flue gas cooler
E-clean flue gas supercharging fan F-chimney
G-flue butterfly valve H-gate valve J-valve
K-butterfly valve L-butterfly valve
Logistics:
1-flue gas to be purified 2-flue gas at the outlet of a dust remover
3-the inlet of the adsorption tower is used for purifying the flue gas, 4-the outlet of the adsorption tower is used for purifying the flue gas
5-draught fan outlet clean smoke 6-chimney clean smoke
7-refluxing and purifying the purified flue gas 8-sending the purified flue gas to a cooler for purifying the flue gas
9-first part of clean flue gas after cooling and 10-second part of clean flue gas after cooling
11-air 12-regenerated coke
13-spent coke 14-nitrogen
Detailed Description
The following detailed description of specific embodiments of the present disclosure is provided in connection with the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present disclosure, are given by way of illustration and explanation only, not limitation.
In the present disclosure, the use of directional words such as "up and down" generally means up and down in the normal use state of the device, unless stated to the contrary. The "inner and outer" are with respect to the outline of the device itself.
The first aspect of the disclosure provides a method for starting up an active coke dry adsorption purification device, which comprises the following steps:
(1) introducing air into an active coke adsorption tower filled with fresh active coke to passivate the fresh active coke;
(2) introducing nitrogen into the activated coke adsorption column to displace at least a portion of the air;
(3) introducing the flue gas to be purified into the active coke adsorption tower, wherein the initial introduction amount of the flue gas to be purified does not exceed 80% of the design load of the device, gradually increasing the introduction amount of the flue gas to be purified until the design load of the device reaches 100%, and normally operating the active coke dry-method adsorption purification device.
According to the start-up method disclosed by the invention, before the flue gas is introduced into the active coke adsorption tower, the active coke is passivated by adopting air circulation, so that the adsorption activity of the active coke is reduced, and the probability of over-temperature of an active coke bed layer is greatly reduced when the flue gas is introduced; meanwhile, after the system is switched into flue gas, the temperature of the flue gas at the inlet of the active coke adsorption tower and the temperature rise of a bed layer of the adsorption tower can be safely and effectively controlled, and the safe and stable operation of the active coke adsorption tower is ensured; by introducing air into the system, the air passivation process of the active coke can be performed in advance independently of an upstream system, the start-up time is shortened, and a convenient condition is created for the start-up of the active coke dry-method purification device; by adopting the start-up method disclosed by the invention, the start-up time of the device can be greatly shortened, and the time can be shortened to be within 2 days from the original 7-10 days.
In the process according to the present disclosure, the "plant design load" is known to the person skilled in the art, i.e. the raw flue gas flow rate which the active coke dry adsorption purification plant is designed to handle.
In accordance with the present disclosure, the activated coke dry adsorption purification device may be conventional in the art, and may include, for example, an activated coke adsorption tower. Further, to avoid excessive temperature rise at the active coke bed and the adsorption column inlet, in one embodiment: the active coke dry method adsorption purification device can comprise an inlet of the flue gas to be purified, an active coke adsorption tower, a flue gas cooler and an outlet of the purified flue gas; the active coke adsorption tower can comprise a gas inlet to be adsorbed, a gas outlet after adsorption and a plurality of active coke adsorption beds, and an interstage gas chamber can be arranged between every two adjacent active coke adsorption beds; an inlet of gas to be adsorbed of the active coke adsorption tower can be communicated with an inlet of the system for flue gas to be purified, an outlet of gas after adsorption of the active coke adsorption tower can be communicated with an outlet of the system for purified flue gas, a purified flue gas circulation pipeline can be arranged between the outlet of gas after adsorption of the active coke adsorption tower and the inlet of gas to be adsorbed of the active coke adsorption tower, an inlet of the purified flue gas circulation pipeline can be communicated with the outlet of gas after adsorption of the active coke adsorption tower, and an outlet of the purified flue gas circulation pipeline can be respectively communicated with the inlet of gas to be adsorbed of the active coke adsorption tower and the interstage gas chamber; the flue gas cooler may be arranged on the clean flue gas recirculation line.
Further, the apparatus of the present disclosure may include a clean flue gas induced draft fan; for example, when the clean flue gas induced draft fan is arranged at the outlet of the active coke adsorption tower, the backflow clean flue gas can be led out from the outlet of the clean flue gas induced draft fan, and at this time, a clean flue gas supercharging fan is not required to be arranged on the clean flue gas backflow flue, as shown in fig. 1, the air inlet is arranged at the inlet of the clean flue gas induced draft fan; when the outlet of the active coke adsorption tower is not provided with the induced draft fan, the backflow clean flue gas is led out from the outlet of the active coke adsorption tower, and a clean flue gas booster fan needs to be arranged on the clean flue gas backflow flue, as shown in fig. 2, the air inlet can be arranged at the inlet of the clean flue gas booster fan.
Furthermore, the inlet of the active coke adsorption tower can be provided with a dust remover, the type of the dust remover can be one of an electric dust remover, a cloth bag dust remover and an electric bag dust remover, and the dust remover can also be omitted.
In order to further improve the passivation effect and efficiency of the air introduced into the adsorption tower on the active coke in the start-up method according to the present disclosure, in one embodiment, a clean flue gas circulation line may be connected between the purified gas outlet of the active coke adsorption tower and the gas inlet to be purified, so that the air introduced into the active coke adsorption tower is subjected to a closed circulation in the adsorption tower, and in this embodiment, the step (1) may include: and circulating the air in the active coke adsorption tower and the clean flue gas circulating pipeline, and gradually increasing the flow of the circulating air until the flow of the circulating air reaches 80-100% of the design load of the device, and then continuously circulating for 12-24 h.
In the start-up method according to the present disclosure, the temperature of the air introduced into the apparatus is not particularly required, and may be, for example, normal temperature air.
In the start-up method according to the present disclosure, after introducing the air circulation passivation active coke into the adsorption tower, the air in the adsorption tower may be replaced by inert gas or nitrogen, and a mixed gas containing nitrogen and air may be obtained at the purified gas outlet of the active coke adsorption tower, in a specific embodiment of the present disclosure, step (2) may include: and stopping introducing the air, returning at least part of the mixed gas into the active coke adsorption tower, discharging the other part of the mixed gas to a chimney, and gradually increasing the flow rate of the mixed gas discharged to the chimney for replacement. The specific operation method can be conventional in the art, for example, after the activated coke adsorption tower completes the air closed cycle according to step (1), a valve on a nitrogen supplementing pipeline of the activated coke adsorption tower can be opened, nitrogen is filled into the activated coke adsorption tower, the closed cycle is continued, and the clean flue gas is gradually opened to a chimney valve to replace the air in the activated coke adsorption tower.
Further, the time for replacement with nitrogen is not particularly limited, and in a preferred embodiment, the replacement in step (2) is performed for 2 hours or more, that is, when the nitrogen introducing time of the system is 2 hours or more and the oxygen content in the gas in the activated coke adsorption tower after sampling analysis is not more than 5 vol%, step (3) is performed to ensure that the nitrogen sufficiently replaces the air in the adsorption tower.
Further, in the start-up method according to the present disclosure, after the nitrogen replacement is completed in the activated coke adsorption tower (the oxygen content in the sampling analysis system is not more than 5 v%), the flue gas to be purified is preferably introduced within 30 minutes to ensure that the oxygen content in the system does not rise significantly during the period.
In the start-up method according to the present disclosure, the step (3) may include two operation stages to introduce the flue gas to be purified into the active coke adsorption tower step by step, and by controlling the flow rate and the operation time of introducing the flue gas to be purified in the two stages, the temperature of the active coke adsorption bed layer may be controlled, the over-temperature phenomenon may be avoided, and the introduction amount of the flue gas to be purified is gradually increased to the design load of the apparatus.
In particular, the first operating phase may comprise: stopping introducing nitrogen, wherein the introduction amount of the flue gas to be purified can be 20-80% of the design load of the device, such as 30-60%; the flue gas discharged from the purified gas outlet of the active coke adsorption tower is divided into a first clean flue gas and a second clean flue gas, the first clean flue gas is cooled by a flue gas cooler and then returns to the active coke adsorption tower for clean flue gas circulation, and the second clean flue gas is discharged to a chimney. In the embodiment, the flue gas cooler is arranged to form a clean flue gas cooling reflux system of the adsorption tower, and the temperatures of the inlet of the active coke adsorption tower and the active coke bed layer can be controlled through the reflux cooling of the clean flue gas, so that the probability of the over-temperature of the active coke bed layer is reduced again.
Further, in the start-up method according to the present disclosure, the active coke adsorption tower may have a multi-stage adsorption bed structure, an inlet air chamber and a plurality of active coke adsorption beds may be sequentially disposed in the active coke adsorption tower along a flue gas flow direction, and an interstage air chamber may be disposed between two adjacent active coke adsorption beds; the step (3) may further include: and returning the first clean flue gas to the inlet air chamber and the interstage air chamber respectively so as to control the temperature of the inlet of the active coke adsorption tower and the active coke bed layer through cooling of the clean flue gas and backflow to the inlet air chamber and the interstage air chamber and avoid the over-temperature of the active coke bed layer.
According to the present disclosure, the active coke adsorption tower may employ a single-stage adsorption bed structure, and may also employ a multi-stage adsorption bed structure, for example, a two-stage adsorption bed structure. Specifically, the method can comprise a single-stage cross-flow bed, a single-stage cross-flow fast-slow bed, a single-stage counter-flow bed, and a double-stage adsorption bed structure, for example, a double-stage cross-flow adsorption bed. For the active coke adsorption tower adopting a single-stage adsorption bed structure, the cooled clean flue gas can return to an inlet flue of the active coke adsorption tower to be mixed with the flue gas to be purified so as to control the inlet flue gas temperature of the active coke adsorption tower; for an active coke adsorption tower adopting a multi-stage adsorption bed structure, for example, an active coke adsorption tower of a two-stage cross-flow adsorption bed structure, the cooled clean flue gas can be divided into a first part of cooled clean flue gas and a second part of cooled clean flue gas: after cooling, the first part of clean flue gas can return to the inlet of the adsorption tower and be mixed with the flue gas to be purified to control the flue gas temperature at the inlet of the active coke adsorption tower, and after cooling, the second part of clean flue gas can return to the inter-stage gas chamber of the active coke adsorption tower to control the bed temperature of the active coke adsorption tower.
In the start-up method according to the present disclosure, the time for performing the first operation stage is not particularly limited, and in a preferred embodiment, when the first operation stage is performed for 12 hours or more and the bed temperature rise of the activated coke adsorption column does not exceed 0.5 ℃ within 1 hour, the activated coke adsorption column is considered to reach a steady state, and the second operation stage may be performed; the second operational phase may include: the introduction amount of the flue gas to be purified is increased to 100% of the design load of the device.
In the start-up method according to the present disclosure, the time for performing the first operation stage is not particularly limited, and in a preferred embodiment, when the second operation stage is performed for more than 6 hours, the total temperature rise of the flue gas passing through the active coke adsorption tower is not more than 15 ℃, and the bed temperature rise after stabilization is not more than 0.5 ℃ within 1 hour, the active coke dry adsorption purification device can normally operate, that is, the start-up of the active coke dry adsorption purification device is completed, and the normal operation can be performed.
In the method of operating according to this disclosure, the method further includes: in the step (3), controlling the temperature of the flue gas to be purified not to be higher than the inlet flue gas temperature of the active coke adsorption tower during normal operation so as to avoid overhigh temperature of a bed layer; further, when the first operation stage and the second operation stage of the step (3) are carried out, the temperature of the flue gas to be purified can be controlled to be not higher than the inlet flue gas temperature of the active coke adsorption tower during normal operation.
In the start-up method according to the present disclosure, the total start-up time may not exceed 48 hours. Wherein the total start-up time refers to the time from the introduction of air into the active coke dry adsorption purification device to the normal operation of the device.
In a preferred embodiment of the start-up method according to the present disclosure, the main process may include: (1) before the active coke adsorption tower is used for introducing flue gas to start working, firstly introducing normal-temperature air into the active coke adsorption tower, closing a clean flue gas to a chimney valve, and opening a clean flue gas circulating system from an outlet of the active coke adsorption tower to an inlet and/or an interstage gas chamber, wherein a flue gas cooler arranged on a clean flue gas circulating pipeline can be unused, air is adopted for closed circulation, the flow of the closed circulating air is gradually increased to 80-100% of the flow of the flue gas to be purified, and the stable operation is not less than 12-24 hours, so that the passivation of fresh active coke is realized, and the reaction activity of the fresh active coke is reduced.
(2) And (2) after the air closed circulation of the active coke adsorption tower is completed according to the step (1), opening a valve on a nitrogen supplementing pipeline of the active coke adsorption tower, filling nitrogen into the active coke adsorption tower, continuing to perform closed circulation, gradually opening clean flue gas to a chimney valve, and replacing the air in the active coke adsorption tower. And entering the next step when the nitrogen introducing time of the system is not less than 2h and the oxygen content in the system is not more than 5 v% after sampling analysis.
(3) After nitrogen replacement is completed in the active coke adsorption tower according to the step (2), introducing smoke to be purified into the system, controlling the temperature of the smoke to be purified to be not more than the smoke temperature of a normal operation inlet, introducing the smoke to be purified to be not more than 80% of the design load (the smoke to be purified) of the system, starting a smoke purification circulating system from an outlet of the active coke adsorption tower to an inlet and/or interstage gas chamber, putting a smoke cooler into use, determining the circulating flow rate and the cooling load of the smoke to be purified according to the temperature rise of the active coke adsorption tower, operating the system for not less than 12 hours after the smoke is introduced, and considering that the active coke adsorption tower reaches a stable state when the temperature rise of a bed layer of the active coke adsorption tower is not more than 0.5 ℃ within 1 hour.
(4) After the active coke adsorption tower reaches a stable state, the amount of flue gas to be purified is increased to 100% of design load, the flue gas temperature is controlled to be not more than the flue gas temperature at a normal operation inlet, at the moment, a flue gas cooler must be put into use, the clean flue gas circulation flow and the cooling load are determined according to the temperature rise of the active coke adsorption tower, after the flue gas is introduced according to the temperature rise, the system operates for not less than 6 hours, the total temperature rise of the flue gas passing through the active coke adsorption tower is not more than 15 ℃, and the temperature rise of a bed layer after the flue gas passes through the active coke adsorption tower is stabilized within 1 hour and is not more than 0.5 ℃, namely the start.
The present disclosure is further illustrated with reference to the following examples, but the present disclosure is not to be construed as being limited thereto.
Example (b):
the active coke dry adsorption purification device shown in figure 1 is adopted, and the start-up method comprises the following steps:
step (1): before the active coke adsorption tower is introduced with flue gas and started, a valve J is opened, a butterfly valve L and a butterfly valve M are opened, a butterfly valve G and a butterfly valve K are closed, a clean flue gas booster fan E is slowly started, normal temperature air 11 is introduced, circulation of air between the active coke adsorption tower B, the clean flue gas booster fan E, a flue gas cooler D and the active coke adsorption tower B is gradually established, then the rotating speed of the clean flue gas booster fan E is gradually increased, and the normal temperature air 11 is continuously introduced. When the rotating speed of the clean flue gas supercharging fan E is close to the design rotating speed and the pressure of the active coke adsorption tower B tends to be stable, the valve J is closed, large-flow closed circulation of air is carried out, the flue gas cooler D is opened, stable operation is not less than 12-24 hours, fresh active coke is passivated, and the adsorption activity of the fresh active coke is reduced.
Step (2): after the active coke adsorption tower B completes air closed circulation according to the step (1), opening the gate valve H, filling nitrogen 14 into the active coke adsorption tower, and performing closed circulation of air and/or nitrogen between the active coke adsorption tower B, the purified flue gas booster fan E, the flue gas cooler D and the active coke adsorption tower B. And simultaneously gradually opening a butterfly valve G to replace the air in the active coke adsorption tower B. And entering the next step when the nitrogen introducing time of the active coke adsorption tower B is not less than 2h and the oxygen content in the system is not more than 5 v% after sampling analysis.
And (3): after the nitrogen replacement is completed in the active coke adsorption tower B according to the step (2), a butterfly valve K is opened, the flue gas to be purified 1 is introduced, the temperature of the flue gas to be purified is 160 ℃ and is not more than the temperature of the flue gas at a normal operation inlet (160-. And (4) putting the flue gas cooler D into service, and adjusting the opening of the butterfly valve L and the butterfly valve M to control the temperature of the inlet of the active coke adsorption tower B and the temperature of the adsorption bed layer. At the moment, the flow of the flue gas to be purified 1, the dust remover A, the active coke adsorption tower B and the chimney F is opened, and a clean flue gas normal establishment circulation is also established between the active coke adsorption tower B, the clean flue gas booster fan E, the flue gas cooler D and the active coke adsorption tower B. After the flue gas 1 to be purified is introduced, the system operates for not less than 12 hours, and the active coke adsorption tower can be considered to reach a stable state when the temperature rise of a bed layer of the active coke adsorption tower B is not more than 0.5 ℃ within 1 hour.
And (4): when the active coke adsorption tower B operates according to the step (3), the amount of the flue gas 1 to be purified is increased to 100% of design load, the temperature of the flue gas is controlled to be not more than the temperature of the flue gas at the inlet of normal operation, the circulation flow of the clean flue gas and the cooling load can be determined according to the temperature rise of the active coke adsorption tower, after the flue gas is introduced according to the design load, the system operates for not less than 6 hours, the total temperature rise of the flue gas passing through the active coke adsorption tower is not more than 15 ℃, and the bed temperature rise is not more than 0.5 ℃ within 1 hour after the flue gas passes through the active coke adsorption tower and is considered to be normal, namely, the.
In the start-up method of the embodiment, the total start-up time is 40h, and the start-up time is greatly shortened; in the process of starting up, the over-temperature phenomenon does not occur on the active coke bed layer; the flue gas temperature at the inlet of the active coke adsorption tower is 160 ℃, and the flue gas temperature between the bed layers (the interstage air chamber) of the adsorption tower is 165 ℃, so that the flue gas temperature between the inlet of the active coke adsorption tower and the bed layers of the adsorption tower can be controlled and reduced, and the bed layers are prevented from being over-heated.
The preferred embodiments of the present disclosure are described in detail with reference to the accompanying drawings, however, the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present disclosure within the technical idea of the present disclosure, and these simple modifications all belong to the protection scope of the present disclosure.
It should be noted that the various features described in the above embodiments may be combined in any suitable manner without departing from the scope of the invention. In order to avoid unnecessary repetition, various possible combinations will not be separately described in this disclosure.
In addition, any combination of various embodiments of the present disclosure may be made, and the same should be considered as the disclosure of the present disclosure, as long as it does not depart from the spirit of the present disclosure.
Claims (10)
1. The method for starting the active coke dry adsorption purification device is characterized by comprising the following steps of:
(1) introducing air into an active coke adsorption tower filled with fresh active coke to passivate the fresh active coke;
(2) passing nitrogen into the activated coke adsorption column to displace at least a portion of the air;
(3) introducing the flue gas to be purified into the active coke adsorption tower, wherein the initial introduction amount of the flue gas to be purified is not more than 80% of the design load of the device, gradually increasing the introduction amount of the flue gas to be purified until the design load of the device is 100%, and normally operating the active coke dry method adsorption purification device.
2. The start-up method of claim 1, wherein a clean flue gas circulation pipeline is connected between the adsorbed gas outlet and the gas inlet to be adsorbed of the active coke adsorption tower, and the step (1) comprises: and circulating the air in the active coke adsorption tower and the clean flue gas circulating pipeline, and gradually increasing the flow of the circulating air until the flow of the circulating air reaches 80-100% of the design load of the device, and then continuously circulating for 12-24 h.
3. The start-up method of claim 1, wherein a mixed gas containing nitrogen and air is obtained at the gas outlet of the activated coke adsorption tower after adsorption, and the step (2) comprises the following steps: and stopping introducing air, returning at least part of the mixed gas into the active coke adsorption tower, discharging the other part of the mixed gas to a chimney, and gradually increasing the flow of the mixed gas discharged to the chimney so as to perform the replacement.
4. The start-up method according to claim 1, wherein the step (3) is performed when the replacement in the step (2) is performed for 2 hours or more and the oxygen content in the gas in the active coke adsorption tower is not more than 5 vol%.
5. The start-up method of claim 1, wherein step (3) comprises:
a first operation stage: stopping introducing nitrogen, wherein the introduction amount of the flue gas to be purified is 20-80% of the design load of the device; and dividing the flue gas discharged from the adsorbed gas outlet of the active coke adsorption tower into a first clean flue gas and a second clean flue gas, cooling the first clean flue gas by a flue gas cooler, returning the first clean flue gas to the active coke adsorption tower for clean flue gas circulation, and discharging the second clean flue gas to a chimney.
6. The start-up method of claim 5, wherein an inlet gas chamber and a plurality of active coke adsorption beds are arranged in the active coke adsorption tower in sequence along the flow direction of flue gas, and an interstage gas chamber is arranged between two adjacent active coke adsorption beds; the step (3) further comprises the following steps: returning the first clean flue gas to the inlet plenum and the interstage plenum, respectively.
7. The start-up method of claim 5, wherein step (3) comprises: when the first operation stage is carried out for more than 12 hours and the temperature of the bed layer of the active coke adsorption tower is not more than 0.5 ℃ within 1 hour, carrying out a second operation stage;
the second operational phase comprises: the introduction of the flue gas to be purified is increased to 100% of the design load of the plant.
8. The start-up method of claim 7, wherein when the second operation stage is carried out for more than 6 hours, the total temperature rise of the flue gas passing through the active coke adsorption tower is not more than 15 ℃, and the bed temperature rise after stabilization is not more than 0.5 ℃ within 1 hour, the active coke dry-method adsorption purification device can normally operate.
9. The method of operating a plant as claimed in any one of claims 1 to 8, wherein the method further comprises: and (4) in the step (3), controlling the temperature of the flue gas to be purified not to be higher than the inlet flue gas temperature of the active coke adsorption tower during normal operation.
10. The method of any one of claims 1 to 8, wherein the total start-up time of the method is not more than 48 hours.
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