CN114471046A - Flue gas purification device and MTO regeneration flue gas purification process system - Google Patents
Flue gas purification device and MTO regeneration flue gas purification process system Download PDFInfo
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- CN114471046A CN114471046A CN202210143165.9A CN202210143165A CN114471046A CN 114471046 A CN114471046 A CN 114471046A CN 202210143165 A CN202210143165 A CN 202210143165A CN 114471046 A CN114471046 A CN 114471046A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8643—Removing mixtures of carbon monoxide or hydrocarbons and nitrogen oxides
- B01D53/8646—Simultaneous elimination of the components
- B01D53/8653—Simultaneous elimination of the components characterised by a specific device
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/404—Nitrogen oxides other than dinitrogen oxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/502—Carbon monoxide
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- 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
Abstract
The invention discloses a flue gas purification device and an MTO regeneration flue gas purification process system, wherein the flue gas purification device comprises a box body with a flue gas inlet and a flue gas outlet, and the bottom of the box body is provided with an ash bucket; the gas purifying device also comprises a partition plate, a plurality of metal filter bags and a catalyst layer, wherein the partition plate is fixed in the box body, a plurality of through holes are formed in the plate body of the partition plate, and the internal cavity of the box body is divided into a gas purifying chamber and a flue gas chamber along a flue gas flow path; the flue gas inlet is arranged at one side of the flue gas chamber, and the flue gas outlet is arranged at one side of the gas purifying chamber; the metal filter bags are respectively arranged in one-to-one correspondence with the through holes, and the bag mouth at the upper end of each metal filter bag is sealed and fixed with the peripheral edge of the corresponding through hole so as to carry out dust removal treatment on the smoke; the catalyst layer is fixed in the air purifying chamber to treat NOx and CO in the flue gas after dust removal treatment. By applying the scheme, dust, NOx and CO generated by the MTO regenerator can be purified simultaneously, and the operation cost is reduced.
Description
Technical Field
The invention relates to the field of flue gas dust removal and environmental protection, in particular to a flue gas purification device and an MTO (methanol to olefins) regeneration flue gas purification process system.
Background
The low-carbon olefins such as ethylene, propylene and the like are important organic chemical raw materials and play an important role in modern petroleum and chemical industries. At present, a Methanol To Olefins (MTO) process is the latest process technology in the coal chemical industry chain, and the process prepares low-carbon olefins by Methanol under the action of a catalyst, and the reaction occurs on the surface of the catalyst and releases a large amount of heat. Meanwhile, the coke which is a byproduct of the reaction is accumulated on the surface of the catalyst, so that the catalyst is quickly deactivated, and the activity of the catalyst can be recovered after the catalyst is subjected to coke burning treatment. The regeneration treatment of the catalyst is carried out in a regenerator, and high-temperature flue gas is generated in the regeneration process and mainly contains carbon monoxide and a large amount of catalyst particles; the high-temperature regenerated flue gas is pretreated by the three-stage cyclone separator, enters the carbon monoxide incinerator for incineration, then enters the waste heat boiler for waste heat recovery, and finally is discharged to the atmosphere through a chimney.
After the high-temperature regenerated flue gas is incinerated in the incinerator, the discharged flue gas contains a large amount of catalyst particle dust, and harmful gases such as NOx, CO and the like are inevitably generated, so that the flue gas needs to be subjected to dust removal treatment in order to reach the emission standard of the atmospheric pollutants required by relevant regulations. In the prior art, the dust removal technology is mature, but the removal technology for NOx and CO needs to be improved, and particularly, the removal technology is influenced by burning raw materials, operation and the like, so that pollutants cannot be effectively intercepted and treated by the conventional flue gas filtering equipment.
In view of the above, it is desirable to optimize the design of the flue gas purification device to overcome the above-mentioned drawbacks.
Disclosure of Invention
In order to solve the technical problems, the invention provides a flue gas purification device and an MTO regeneration flue gas purification process system, which simultaneously purify dust, NOx and CO generated by an MTO regenerator through scheme optimization and reduce the operation cost.
The invention provides a flue gas purification device, which comprises a box body with a flue gas inlet and a flue gas outlet, wherein an ash hopper is arranged at the bottom of the box body; the gas purification device also comprises a partition plate, a plurality of metal filter bags and a catalyst layer, wherein the partition plate is fixed in the box body, a plurality of through holes are formed in a plate body of the partition plate, and an internal cavity of the box body is divided into a gas purification chamber and a flue gas chamber along a flue gas flow path; the flue gas inlet is arranged on one side of the flue gas chamber, and the flue gas outlet is arranged on one side of the gas purifying chamber; the metal filter bags are respectively arranged corresponding to the through holes one by one, and a bag opening at the upper end of each metal filter bag is hermetically fixed with the peripheral edge of the corresponding through hole so as to carry out dust removal treatment on the smoke; the catalyst layer is fixed in the air purifying chamber to treat NOx and CO in the flue gas after dust removal treatment.
Optionally, the dust removing device further comprises a blowing dust removing device arranged above the partition plate to output dust removing gas to the plurality of metal filter bags.
Optionally, the cross section of the metal filter bag is star-shaped.
Optionally, the metal filter bag comprises a reinforcing mesh body and at least two fiber layers, the at least two fiber layers are sequentially laid on the reinforcing mesh body and sintered to form a filter felt body, and the fiber diameters of the at least two fiber layers are configured as follows: the diameter of the fibers in the outer layer is smaller than the diameter of the fibers in the inner layer.
Optionally, the reinforcing mesh body is formed by weaving steel wires with the diameter of 0.1 mm-0.2 mm.
Optionally, the at least two fiber layers comprise an outer fine fiber layer and an inner coarse fiber layer, both of which are metal fibers, the fiber diameter of the outer fine fiber layer is 5 μm to 10 μm, and the fiber diameter of the inner coarse fiber layer is 20 μm to 30 μm.
Optionally, the catalyst layer includes a supporting beam fixedly connected to the box body, the supporting beam is integrally in a grid shape, a catalyst block is placed in each grid, and the catalyst block includes a carrier and a catalyst attached to the carrier is a Pd-Rh composite catalyst.
Optionally, the pitch of the catalyst block is configured to be 3.7mm to 5.9 mm.
The invention also provides an MTO regeneration flue gas purification process system which comprises a regenerator, a separator, a CO incinerator, a waste heat boiler, an ammonia water tank and the flue gas purification device which are sequentially communicated.
Optionally, the method further comprises: a high-pressure blower, an air outlet of which is communicated with the upstream end of the CO incinerator; the flue gas water-sealed tank is communicated between the separator and the CO incinerator and between the flue gas purification device and the chimney; the heat recovery device and the smoke baffle door are sequentially communicated and arranged between the smoke purification device and the chimney.
Compared with the prior art, the invention provides a smoke purification device capable of simultaneously purifying dust, NOx and CO generated by an MTO regenerator, the scheme utilizes the partition plate to divide the internal cavity of the box body into the air purifying chamber and the smoke chamber, the metal filter bag used for dedusting the smoke is positioned in the smoke chamber, and the catalyst layer is fixed in the air purifying chamber to treat the NOx and CO in the smoke after dedusting treatment. So set up, this scheme has following beneficial technological effect:
firstly, the scheme integrates the functions of dust removal treatment and NOx and CO removal treatment in the flue gas, and has small occupied area and small volume; the metal filter bag is high-temperature resistant, long in service life and recyclable, and can be used for a long time under the working condition of below 800 ℃ according to different metal fibers, so that the possibility of burning the filter bag when CO is not completely burned in the incinerator to cause tail combustion can be avoided. On the whole, have compact structure and economic nature excellent characteristics.
Secondly, based on the characteristic that the catalyst is placed on the downstream side of dust removal in the scheme, the catalyst is arranged after the metal filter bag is subjected to high-temperature dust removal, the adverse effect of fly ash is basically eliminated, and the using amount of the catalyst can be effectively reduced. Through production trial production, the service life of the catalyst can be prolonged to 5-6 years, the dosage is reduced by more than 1/2, the ammonia escape is reduced, and the investment and operation cost is reduced.
Thirdly, in an alternative of the invention, the cross-section of the metal filter bag is star-shaped. Therefore, based on the same length of the filter bag, the filtering area of the filter bag can be greatly increased, and the height of the box body of the purifying device is reduced, so that the volume of the purifying device is reduced, and the cost is reduced; in addition, the star-shaped section can reduce the rising speed of the flue gas, reduce secondary dust raising and improve the dust cleaning performance of the filter bag. In addition, the filter bag adopts the star cross section, compares with conventional straight section filter bag, under the unchangeable circumstances of filter area, can shorten the length of filter bag, can reduce the resistance in the deashing treatment process, even if extrude into finer catalyst granule dust in the metal filter bag micropore, also can effectively improve the deashing effect, and filter accuracy is higher.
Fourthly, in another preferred embodiment of the present invention, the filter felt body of the metal filter bag is formed by sintering micron-sized metal fibers after gradient layering of an ultrafine fiber layer and a coarse fiber layer, and specifically includes a reinforcing mesh body and at least two fiber layers, and the fiber diameters of the at least two fiber layers are configured as follows: the diameter of the fibers in the outer layer is smaller than the diameter of the fibers in the inner layer. In this way, the fine fiber layer and the coarse fiber layer are used to achieve the filtering effect, and the reinforcing net is used to improve the warp and weft strength of the filtering felt body. After the gradient layering, the integral filter felt is sintered and combined, and has the characteristics of high filtration precision, low resistance, good ash removal performance and high strength.
Fifthly, in still another preferred aspect of the present invention, the catalyst layer provides a base structure with a supporting beam in a grid shape, and a catalyst block is placed in each grid, and the catalyst attached to the carrier of the catalyst block is a Pd — Rh composite catalyst. The Pd-Rh composite catalyst has high activity and high stability, and the removal and conversion effect is better and can reach more than 90 percent.
Finally, the MTO regeneration flue gas purification process system provided by the invention is characterized in that a flue gas purification device is arranged behind a waste heat boiler and in front of a chimney, and an air outlet of a high-pressure blower of the flue gas purification device is communicated with the upstream end of the CO incinerator; that is, a high pressure blower is provided in front of the CO incinerator to supply O to the CO incinerator2And meanwhile, the smoke purifying device can work in a positive pressure state, and a draught fan is not needed to be arranged at the downstream of the smoke purifying device, so that the phenomenon of condensation caused by condensation when external low-temperature air enters the smoke purifying device can be avoided. In addition, the dedusting process system of the MTO regenerated flue gas is simplified, and the energy consumption can be further reduced。
Drawings
FIG. 1 is a flow diagram of a process system for the purification of MTO regeneration flue gas in an embodiment;
FIG. 2 is a schematic diagram of the overall structure of the flue gas purification device in the embodiment;
FIG. 3 is a schematic structural diagram of a metal filter bag according to an embodiment;
FIG. 4 is a schematic cross-sectional view of the metal filter bag shown in FIG. 3;
fig. 5 is an enlarged view of a portion a of fig. 4.
In the figure:
the system comprises a regenerator 1, a cyclone separator 2, a flue gas water seal tank 31, a flue gas water seal tank 32, a high-pressure blower 4, a CO incinerator 5, a waste heat boiler 6, an ammonia water tank 7, a flue gas purification device 8, a heat recovery device 9, a flue gas baffle door 10 and a bypass flue gas baffle door 11;
the device comprises a box body 81, a flue gas inlet 811, a flue gas outlet 812, a gas purifying chamber 81a, a flue gas chamber 81b, an ash hopper 82, a support frame 83, a metal filter bag 84, a reinforcing mesh body 841, an inner layer coarse fiber layer 842, an outer layer fine fiber layer 843, a bag mouth flange 844, a catalyst layer 85, a catalyst block 851, a support beam 852, a partition plate 86, a through hole 861, a blowing ash removal device 87 and a compressed nitrogen pipeline 88.
Detailed Description
In order to make the technical solutions of the present invention better understood by those skilled in the art, the present invention will be further described in detail with reference to the accompanying drawings and specific embodiments.
Without loss of generality, the present embodiment takes the system configuration shown in fig. 1 as a basis for description, and the detailed description is directed to the flue gas purification device solution. The flue gas dust removal system comprises a regenerator 1, a cyclone separator 2, a CO incinerator 5, a waste heat boiler 6, an ammonia water tank 7, a flue gas purification device 8 and a heat recovery device 9 which are sequentially communicated, and flue gas subjected to purification treatment is discharged into the atmosphere through a chimney. Wherein, the flue gas purification device 8 is arranged at the downstream side of the waste heat boiler 6 and at the upstream side of the chimney.
The terms "upstream" and "downstream" are used herein to define the direction of flue gas flow within the system, it being understood that the use of the terms is merely used to clearly illustrate the principles of operation of the present solution and is not intended to be a substantial limitation on the scope of the claims.
As shown in fig. 1, the flue gas to be treated enters a regenerator 1 for regeneration treatment, the regenerated flue gas is pre-dedusted by a cyclone separator 2 and then enters a CO incinerator 5 for combustion, and the incinerated high-temperature flue gas (the temperature is about 1000 ℃) is subjected to heat recovery by a waste heat boiler 6, and the temperature can be controlled between 300 ℃ and 450 ℃; the high temperature flue gas containing dust, NOx and CO is filtered and removed by the flue gas purification device 8, enters the heat recovery device 9 to recover heat, and is finally discharged through a chimney, so that the purification process is completed. In the scheme, the denitration reducing agent adopts ammonia water stored in an ammonia water tank 7, for example, but not limited to, 20% ammonia water is sprayed into a flue in front of a flue gas purification device 8 through a metering pump and an atomizing nozzle, the ammonia water is gasified by utilizing high-temperature flue gas, and after the ammonia gas and the flue gas are fully and uniformly mixed in the flue gas purification device 8, NOx is reduced into N under the action of a catalyst2While oxidizing CO to CO2。
Here, the heat recovery device 9 can be selected and matched according to the system design, so that further waste heat recovery is performed before the flue gas is discharged into the atmosphere, and the emission requirements of energy conservation and environmental protection are met. Certainly, according to the actual system configuration of the flue gas to be treated, a flue gas water seal tank can be arranged, the flue gas water seal tank is communicated and arranged between the cyclone separator 2 and the CO incinerator 5, and between the flue gas purification device 8 and the chimney, and the flue gas can be completely isolated to prevent CO leakage and backfire. Specifically, as shown in the figure, the flue gas water seal tank 31 is arranged between the cyclone separator 2 and the CO incinerator 5 in a communicating manner, and the flue gas water seal tank 32 is arranged between the flue gas purification device 8 and the chimney in a communicating manner.
In addition, the downstream end of the heat recovery device 9 may be provided with a flue gas damper 10 to be turned off or on as required for system operation. In addition, a bypass flue can be arranged between the outlet of the cyclone separator 2 and the inlet of the chimney, and is controlled to be closed or opened through a bypass flue gas damper 11, and the bypass flue gas damper is normally in a closed state, so that flue gas in the flue can be divided and adjusted according to the operation requirement of the system.
Wherein, the flue gas purification device 8 works in a high temperature environment of approximately 300-450 ℃, if the external low temperature air enters the flue gas purification device 8, the dew condensation is easy to occur, and the performance of the flue gas purification device 8 is affected. Therefore, the MTO regeneration flue gas purification process system provided by the scheme is provided with a high-pressure blower 4 at the upstream end of a CO incinerator 5 to provide O2To the CO incinerator 5.
The term "high-pressure blower" used herein means that the high-pressure air output by the high-pressure blower enables the flue gas cleaning device 8 to operate in a positive pressure state, and there is no need to provide an induced draft fan downstream of the flue gas cleaning device 8. So set up, can avoid external low temperature air to get into in the gas cleaning device 8 and take place the condensation phenomenon of dewing, the system can be simplified simultaneously, can further reduce the energy consumption.
Wherein, the flue gas cleaning device 8 comprises a box 81, the box 81 comprises a flue gas inlet 811 and a flue gas outlet 812, and the bottom of the box 81 is provided with an ash hopper 82. Referring to fig. 2, a schematic diagram of the overall structure of the flue gas purification device in the present embodiment is shown.
As shown in the drawing, the housing 81 is provided on a support frame 83 to facilitate the arrangement of the fitting space. The flue gas flowing out of the waste heat boiler 6 enters the box 81 through the flue gas inlet 811, and is discharged through the flue gas outlet 812 after being subjected to dust removal by the metal filter bag 84 and treatment of removing NOx and CO by the catalyst layer 85 in sequence.
In this embodiment, a partition plate 86 fixed inside the housing 81 forms a basic physical partition, and divides the internal chamber of the housing 81 into a purge chamber 81a and a flue gas chamber 81b along the flue gas flow path. The partition plate 86 is provided with a plurality of through holes 861, and accordingly, the flue gas inlet 811 is disposed on the flue gas chamber 81b side and the flue gas outlet 812 is disposed on the purge chamber 81a side.
The metal filter bags 84 are respectively in one-to-one correspondence with the through holes 861, the upper end opening and the lower end of each metal filter bag 84 are closed, and the upper end opening and the periphery of the corresponding through hole 861 are fixed in a sealing mode so as to perform dust removal treatment on the smoke. That is, the metal filter bag 84 is suspended in the through hole 861 of the partition plate 86. Please refer to fig. 3, which is a schematic structural diagram of the metal filter bag according to the present embodiment.
The bag mouth of the metal filter bag 84 is provided with a bag mouth flange 844, and in specific application, the bag mouth flange 844 of the metal filter bag 84 can be pressed on the through hole 861 edge surface of the partition plate 86 by a pressing block for sealing and fixing. It can be understood that the sealing and fixing manner between the metal filter bag 84 and the corresponding penetration hole 861 can be selected according to the actual product design, as long as good sealing and reliable fixing can be achieved.
In order to further improve the dust cleaning effect and the filtering precision, the cross section of the metal filter bag 84 in the scheme is in a star shape. Please refer to fig. 4, which is a schematic cross-sectional view of the metal filter bag shown in fig. 3.
As shown in the figure, the cross section of the metal filter bag 84 is in a star shape, and the outline is in smooth transition, so that the manufacturability is better. Therefore, based on the same length of the filter bag, the filtering area of the filter bag can be greatly increased, and the height of the box body of the purifying device is reduced, so that the volume of the purifying device is reduced, and the cost is reduced; in addition, the star-shaped section can reduce the rising speed of the flue gas, reduce secondary dust raising and improve the dust cleaning performance of the filter bag. In addition, the filter bag adopts the star cross section, compares with conventional straight section filter bag, under the unchangeable circumstances of filter area, can shorten the length of filter bag, can reduce the resistance in the deashing treatment process, even if extrude into finer catalyst granule dust in the metal filter bag micropore, also can effectively improve the deashing effect, and filter accuracy is higher.
Further, the metal filter bag 84 comprises a reinforcing mesh body 841 and at least two fiber layers, wherein the at least two fiber layers are sequentially laid on the reinforcing mesh body 841 and sintered to form a filter felt body, namely a filter bag body. Wherein the fiber diameters of the at least two fiber layers are configured as follows: the diameter of the fibers in the outer layer is smaller than the diameter of the fibers in the inner layer. Please refer to fig. 5, which is an enlarged view of a portion a of fig. 4.
Such as but not limited to the two fiber layers shown in the figures, as a preferred example to characterize the relative relationship of the fiber layers to the reinforcing mesh body. Here, the outer fine fiber layer 843 and the inner coarse fiber layer 842 are both metal fibers, the fiber diameter of the outer fine fiber layer 843 may be 5 to 10 μm, and the fiber diameter of the inner coarse fiber layer 842 may be 20 to 30 μm. In other words, the filtering felt body of the metal filter bag 84 is formed by sintering a micron-sized metal fiber after gradient layering of a superfine fiber layer and a crude fiber layer, wherein the gradient layering comprises from outside to inside: the superfine fiber layer (the outer fine fiber layer 843) → the coarse fiber layer (the inner coarse fiber layer 842) → the reinforcing mesh body 841, the superfine fiber and the coarse fiber are all prepared in a drawing mode, and the fine fiber layer and the coarse fiber layer are utilized to achieve a filtering effect.
Wherein, the reinforcing mesh 841 can be formed by weaving steel wires with the diameter of 0.1 mm-0.2 mm, and the warp and weft strength of the filtering felt body is improved by the reinforcing mesh. After the gradient layering, the integral filter felt is sintered and combined, and has the characteristics of high filtration precision, low resistance, good ash removal performance and high strength.
In this embodiment, the catalyst layer 85 is fixed inside the air purifying chamber 81a to treat NOx and CO in the flue gas after the dust removal treatment. Based on the characteristic that the catalyst is placed on the downstream side of the dust removal, the catalyst is arranged after the metal filter bag removes dust at high temperature, the adverse effect of fly ash is basically eliminated, and the using amount of the catalyst can be effectively reduced.
Specifically, catalyst block 851 may be placed on support beam 852. The catalyst block 851 comprises a carrier and a catalyst attached to the carrier, and in this embodiment, a Pd-Rh composite catalyst is used, for example, but not limited to, the composite ratio of Pd to Rh is 1:1, so as to obtain a better conversion removal effect.
In a specific implementation, support beams 852 provide the basic function of supporting catalyst blocks 851, which are fixedly attached to housing 81. The support beam 81 is in a grid shape as a whole, catalyst blocks 851 are placed in each grid, and a Pd-Rh composite catalyst is attached to a carrier of each catalyst block. The Pd-Rh composite catalyst has high activity and high stability, and the removal and conversion effect is better and can reach more than 90 percent.
In order to reduce the amount of catalyst used, the pitch of the catalyst block 851 in this embodiment is preferably set to 3.7mm to 5.9 mm. Through production trial production, the resistance can be controlled to be less than 500Pa, the service life of the catalyst can be prolonged to 5-6 years, the use amount is reduced by more than 1/2, the ammonia escape is reduced, and the investment and operation cost is reduced. The pitch of the catalyst block 851 as used herein means the distance between the geometric centers of two adjacent catalyst blocks 851.
In the scheme, a pulse-jet ash removal device 87 is arranged above the metal filter bag 84 and used for removing ash from the metal filter bag 84. As shown in fig. 2, the blowing ash removal device 87 is disposed above the partition plate 86 to output the ash removal gas to the plurality of metal filter bags.
In a specific implementation, the pulse-jet ash removal device 87 is connected with an air source through a compressed nitrogen pipeline 88, so as to provide the air source for the pulse-jet ash removal device 90. Here, the blowing ash removal device 87 can be implemented in different structures according to specific product designs. It should be understood that the blowing ash removal device 87 is not the core invention of the present application and can be implemented by those skilled in the art based on the prior art, and therefore, the detailed description thereof is omitted here.
On the whole, the scheme integrates the functions of dust removal treatment and NOx and CO removal treatment in the flue gas, and has small occupied area and small volume; the metal filter bag is high-temperature resistant, long in service life and recyclable, and can be used for a long time under the working condition of below 800 ℃ according to different metal fibers, so that the possibility of burning the filter bag when CO is not completely burned in the incinerator to cause tail combustion can be avoided. Has the characteristics of compact structure and excellent economical efficiency.
It should be noted that the system employed in the embodiment of the present application is configured as follows: the system comprises a regenerator 1, a cyclone separator 2, a flue gas water seal tank 3, a high-pressure blower 4, a CO incinerator 5, a waste heat boiler 6, an ammonia water tank 7, a heat recovery device 9, a flue gas baffle door 10, a bypass flue gas baffle door 11 and the like.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that it is obvious to those skilled in the art that various modifications and improvements can be made without departing from the principle of the present invention, and these modifications and improvements should also be considered as the protection scope of the present invention.
Claims (10)
1. A flue gas purification device comprises a box body with a flue gas inlet and a flue gas outlet, wherein an ash hopper is arranged at the bottom of the box body; it is characterized by also comprising:
the partition plate is fixed inside the box body, and divides an internal cavity of the box body into a gas purifying chamber and a flue gas chamber along a flue gas flow path; the flue gas inlet is arranged on one side of the flue gas chamber, and the flue gas outlet is arranged on one side of the gas purifying chamber;
the metal filter bags are respectively arranged in one-to-one correspondence with the through holes, and the bag mouth at the upper end of each metal filter bag is hermetically fixed with the peripheral edge of the corresponding through hole so as to carry out dust removal treatment on the smoke;
and the catalyst layer is fixed in the air purifying chamber to treat NOx and CO in the flue gas after dust removal treatment.
2. The flue gas purification apparatus according to claim 1, further comprising:
and the blowing dust removal device is arranged above the partition plate so as to output dust removal gas to the plurality of metal filter bags.
3. The flue gas purification device according to claim 1 or 2, wherein the cross section of the metal filter bag is star-shaped.
4. The flue gas purification device according to claim 3, wherein the metal filter bag comprises a reinforcing mesh body and at least two fiber layers, the at least two fiber layers are sequentially laid on the reinforcing mesh body and sintered to form a filter felt body, and the fiber diameters of the at least two fiber layers are configured as follows: the diameter of the fibers in the outer layer is smaller than the diameter of the fibers in the inner layer.
5. The flue gas purification device according to claim 4, wherein the reinforcing mesh body is formed by weaving steel wires with the diameter of 0.1-0.2 mm.
6. The flue gas purification device according to claim 5, wherein the at least two fiber layers comprise an outer fine fiber layer and an inner coarse fiber layer, both of which are metal fibers, the fiber diameter of the outer fine fiber layer is 5 μm to 10 μm, and the fiber diameter of the inner coarse fiber layer is 20 μm to 30 μm.
7. The flue gas purification device according to claim 4, wherein the catalyst layer comprises a support beam fixedly connected with the box body, the support beam is integrally in a grid shape, a catalyst block is placed in each grid, and the catalyst block comprises a carrier and a catalyst attached to the carrier is a Pd-Rh composite catalyst.
8. The flue gas purification apparatus according to claim 7, wherein the pitch of the catalyst block is configured to be 3.7mm to 5.9 mm.
9. An MTO regeneration flue gas purification process system is characterized by comprising a regenerator, a separator, a CO incinerator, a waste heat boiler, an ammonia water tank and a flue gas purification device which are sequentially communicated; wherein the flue gas purification device adopts the flue gas purification device of any one of claims 1 to 8.
10. The MTO regeneration flue gas purification process system according to claim 9, further comprising:
the air outlet of the high-pressure blower is communicated with the upstream end of the CO incinerator;
the flue gas water-sealed tank is communicated between the separator and the CO incinerator and between the flue gas purification device and the chimney;
the heat recovery device and the smoke baffle door are sequentially communicated and arranged between the smoke purification device and the chimney.
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Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
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