阅读说明：本技术 一种双区布料烟气脱酸方法和系统 (Double-area distribution flue gas deacidification method and system ) 是由 张延虎 于鲁豫 杜伟 吕文涛 杨同涛 王湘宇 姜科 董海洋 王永涛 姜晓菲 王燕 于 2021-09-23 设计创作，主要内容包括：本发明提供了一种双区布料烟气脱酸方法和系统,涉及烟气脱酸技术领域,以解决现有技术中传统的烟气脱酸工艺除酸效率低的问题,该脱酸方法包括将初始脱酸剂与系统烟气路径后端的含低浓度酸性化合物的烟气进行一次反应；将一次反应后的烟气进行除尘处理,除尘处理过程中烟气与一次反应后的脱酸剂进行二次反应；将二次反应后的脱酸剂返回至系统烟气路径前端并与初始烟气进行三次反应；经过三次反应后的脱酸剂与烟气进行充分接触形成四次反应。本发明的双区布料烟气脱酸方法和系统有效提高了烟气中酸性化合物的脱除效率,提高脱酸剂的利用率,脱酸系统运行阻力小,烟气路径短。(The invention provides a double-zone cloth flue gas deacidification method and a double-zone cloth flue gas deacidification system, which relate to the technical field of flue gas deacidification and aim to solve the problem of low deacidification efficiency of the traditional flue gas deacidification process in the prior art, wherein the deacidification method comprises the steps of carrying out primary reaction on an initial deacidification agent and flue gas containing low-concentration acidic compounds at the rear end of a flue gas path of the system; performing dust removal treatment on the flue gas after the primary reaction, and performing secondary reaction on the flue gas and the deacidification agent after the primary reaction in the dust removal treatment process; returning the deacidification agent after the secondary reaction to the front end of the flue gas path of the system and carrying out tertiary reaction with the initial flue gas; the deacidification agent after the three reactions is fully contacted with the smoke to form four reactions. The dual-zone material distribution flue gas deacidification method and the dual-zone material distribution flue gas deacidification system effectively improve the removal efficiency of acidic compounds in the flue gas, improve the utilization rate of deacidification agents, and have the advantages of small running resistance of the deacidification system and short flue gas path.)

1. A double-zone cloth flue gas deacidification method is characterized by comprising the following steps:

carrying out primary reaction on the initial deacidification agent and the flue gas containing the low-concentration acidic compound at the rear end of the flue gas path of the system;

performing dust removal treatment on the flue gas subjected to the primary reaction so as to perform secondary reaction on the flue gas and a deacidification agent in the dust removal treatment process;

returning the deacidification agent subjected to the secondary reaction to the front end of a system flue gas path and carrying out tertiary reaction with the initial flue gas;

carrying out rotary flow on the deacidification agent after the three reactions and the flue gas to ensure that the deacidification agent and the flue gas are fully contacted to carry out four reactions; wherein, the flue gas containing low-concentration acidic compounds in the first reaction is the flue gas after the fourth reaction.

2. The dual zone fabric flue gas deacidification method according to claim 1, further comprising:

transporting the deacidification agent which has undergone the fourth reaction and is fully reacted out of the reaction system, an

One part of the deacidification agent which is not completely reacted is subjected to dust removal treatment under the driving of flue gas flow, and the other part of the deacidification agent and the deacidification agent after the secondary reaction are subjected to the third reaction together in a circulating manner.

3. The dual-zone cloth flue gas deacidification method according to claim 1, wherein the deacidification agent is Al₂O₃Powder or calcium-based acid scavenger or sodium-based acid scavenger, said Al₂O₃The specific surface area a of the powder satisfies a condition that a is more than or equal to 35m²The mesh number b of the sodium-based acid scavenger particles is more than or equal to 500 meshes, and the calcium-based acid scavenger is quicklime or slaked lime.

4. A dual-zone distribution flue gas deacidification system is characterized in that the deacidification system is used for realizing the deacidification method according to any one of claims 1 to 3, and comprises a material gasification bed (10), a material circulation regulation and control device (3), a material feeding device (2), and a reaction air pipe (4), a vortex synergistic reactor (5), an air equalizing device (6) and a dust removing device (7) which are sequentially arranged along the flue gas conveying direction,

the air equalizing device (6) is communicated with the vortex synergistic reactor (5), a feeding pipeline (21) of the material feeding device (2) penetrates through a wall plate of the air equalizing device to extend to the upper side of the air equalizing device (6) and carries out primary reaction on an initial deacidification agent and the flue gas containing low-concentration acidic compounds flowing out of the vortex synergistic reactor (5);

the dust removal device (7) is arranged above the air equalizing device (6), a filter bag used for filtering particles is arranged on the dust removal device (7), a reaction ash layer which is driven by the rising of the flue gas and attached to the particles is formed on the surface layer of the filter bag, so that in the process that the flue gas after primary reaction passes through the filter bag of the dust removal device (7), an acidic compound in the flue gas and a deacidification agent in the reaction ash layer are subjected to secondary reaction;

the material gasification bed (10) is arranged below the air equalizing device (6), one end of the material circulation regulation and control device (3) is connected with the material gasification bed (10), and the other end of the material circulation regulation and control device is connected with the reaction air pipe (4), so that the deacidification agent after the secondary reaction is conveyed into the reaction air pipe (4) and is subjected to a tertiary reaction with the initial flue gas;

the reaction air pipe (4) is connected to the lower end of the vortex synergistic reactor (5), the flue gas and the deacidification agent passing through the reaction air pipe (4) rise into the vortex synergistic reactor (5), and the flue gas and the deacidification agent are fully contacted in the vortex synergistic reactor (5) to carry out four times of reaction.

5. The dual-zone distribution flue gas deacidification system according to claim 4, wherein a material distributing plate (101) is arranged in the material gasification bed (10), the material distributing plate (101) divides the interior of the material gasification bed (10) into a circulation zone (103) and a return zone (102), the material circulation regulating and controlling device (3) is connected with the circulation zone (103) of the material gasification bed, and the return zone (102) of the material gasification bed is connected with an external return conveying device (9).

6. The dual-zone material distribution flue gas deacidification system according to claim 4, wherein a gasification plate (104) is arranged in the material gasification bed (10), external air flows into the material gasification bed through the gasification plate (104), the gasification plate (104) is made of a flexible woven material, and the gasification plate (104) is capable of permeating gas and blocking powder particles.

7. The dual-zone cloth flue gas deacidification system according to claim 4, wherein the air equalizing device (6) comprises a shell (64), a second baffle plate (62), a third baffle plate (63) and a plurality of first baffle plates (61), the second baffle plates (62) and the third baffle plates (63) are arranged in the shell (64), the plurality of first baffle plates (61) are connected to the second baffle plate (62) at intervals, a vertical channel is formed between every two adjacent first baffle plates (61), one side of each first baffle plate (61) departing from the second baffle plate (62) is connected to the upper side of the air outlet (59) of the vortex synergistic reactor (5), and the third baffle plate (63) is arranged on the shell (64) relative to the second baffle plate (62).

8. The dual-zone distribution flue gas deacidification system according to claim 4, wherein the vortex synergistic reactor (5) comprises a shell (51) and an outer arc plate (52), the outer arc plate (52) and the shell (51) form a synergistic chamber with an arc arch structure, a first vortex plate (53), a first guide plate (55), a second guide plate (56), a material homogenizing plate (57) and a second vortex plate (54) are arranged in the synergistic chamber, the first vortex plate (53), the first guide plate (55) and the second guide plate (56) are all arc structures, the first vortex plate (53) is arranged at an inlet end, the first guide plate (55) and the second guide plate (56) are distributed in parallel and are both arranged opposite to the first vortex plate (53), the second vortex plate (54) is arranged below the first guide plate (55) and the second guide plate (56), the homogenizing plate (57) is arranged at the outlet end.

9. The dual-zone distribution flue gas deacidification system according to claim 4, wherein a plurality of material diffusers (13) are arranged in the reaction air duct (4), and a plurality of material diffusers (13) are arranged along the wall of the reaction air duct (4);

the tail end of a feeding pipeline (21) of the material feeding device (2) is provided with a material diffuser so as to uniformly distribute the deacidification agent in the air equalizing device (6).

10. The dual-zone cloth flue gas deacidification system according to claim 4, further comprising a supporting frame (17), wherein the dust removing device (7) is arranged on the upper side of the supporting frame (17), the air equalizing device (6) is embedded in the supporting frame (17), the side part of the dust removing device (7) is connected with the outlet flue (8), the lower end of the reaction air pipe (4) is connected with the inlet flue (15), and the inlet flue (15) and the outlet flue (8) are provided with valves.

Technical Field

The invention relates to the technical field of flue gas deacidification, in particular to a double-area cloth flue gas deacidification method and a double-area cloth flue gas deacidification system.

Background

The treatment of flue gas containing acidic compounds in industrial production engineering is becoming the focus of industry, and the environmental air quality standard (GB3095-2012) is also implemented nationwide in 2016, 1/1. Acidic compounds are one of the traditional atmospheric pollutants. Driven by a new policy that economy, society and environment need to be coordinately developed, the method needs to be enhanced to carry out high-efficiency treatment on the plant.

At present, the wet process which is more applied is easy to generate secondary pollution, white smoke exists at the outlet of a chimney and is gradually abandoned, and the dry semi-dry deacidification process also has CFB, RCFB, SDA and GSA processes, and has the following defects: the CFB and RCFB processes have poor acid removal adaptability, a bed layer needs to be established for reaction, bed collapse accidents often occur, the system resistance is large, the feeding is uneven, even if the improved multipoint feeding technology is used on the basis, local material imbalance can be caused, the reaction of the deacidification agent is incomplete, the deacidification agent is quick to lose efficacy, the ratio of raw material components in the deacidification product is too high, and the deacidification agent material is seriously wasted. The deacidification in SDA and GSA processes is carried out by spraying deacidification agent into the system in the form of slurry to be mixed with flue gas for deacidification reaction, and the process needs to strictly control the amount of the sprayed slurry, so that the problems of caking, blockage and the like are easily caused, further a subsequent dedusting system is influenced, and the problem of large system resistance is also caused.

In the conventional flue gas deacidification process, as shown in fig. 1 and 2, a fresh initial deacidification agent is added into a reaction air duct 4 at an inlet of a system and reacts with initial flue gas containing high-concentration acidic compounds entering through an inlet flue 15, and the reacted flue gas enters a chimney 14 through a dust removal device 7 under the action of a smoke exhaust fan 12 and is discharged out of the system; the deacidification agent is blocked by the dust removal device 7, the deacidification agent which is not completely reacted is circularly returned to the reaction air pipe 4 through the feeding device 2, and the deacidification agent which is completely reacted is conveyed to the product bin 11 through the return conveying device 9. However, the deacidification process has the advantages of long flue gas path, large system resistance, serious equipment abrasion, low deacidification agent utilization rate, quick failure and low deacidification efficiency, and can not meet the national requirements on energy conservation, emission reduction and consumption reduction.

Disclosure of Invention

The invention aims to provide a double-zone cloth flue gas deacidification method and a double-zone cloth flue gas deacidification system, which aim to solve the problem of low deacidification efficiency of the traditional flue gas deacidification process in the prior art.

The invention provides a double-area cloth flue gas deacidification method which comprises the following steps:

carrying out primary reaction on the initial deacidification agent and the flue gas containing the low-concentration acidic compound at the rear end of the flue gas path of the system;

performing dust removal treatment on the flue gas subjected to the primary reaction so as to perform secondary reaction on the flue gas and an acid removal agent in the dust removal treatment process;

returning the deacidification agent subjected to the secondary reaction to the front end of a system flue gas path and carrying out tertiary reaction with the initial flue gas;

carrying out rotary flow on the deacidification agent after the three reactions and the flue gas to ensure that the deacidification agent and the flue gas are fully contacted to carry out four reactions; wherein, the flue gas containing low-concentration acidic compounds in the first reaction is the flue gas after the fourth reaction.

As a preferred aspect of the present invention, the method further comprises: conveying the deacidification agent which has undergone the four reactions and is fully reacted out of the reaction system, an

And (3) carrying out dust removal treatment on one part of the deacidification agent which is not completely reacted under the driving of flue gas flow, and carrying out the third reaction together with the deacidification agent after the second reaction in a circulating manner.

In a preferred embodiment of the present invention, the deacidification agent is Al₂O₃Powder or calcium-based acid scavenger or sodium-based acid scavenger, said Al₂O₃The specific surface area a of the powder satisfies a condition that a is more than or equal to 35m²The number b of the sodium-based acid scavenger particles is more than or equal to 500 meshes, and the calcium-based acid scavenger is quicklime or slaked lime.

The invention also provides a dual-zone distribution flue gas deacidification system, which is used for realizing the deacidification method and comprises a material gasification bed, a material circulation regulation and control device, a material feeding device, and a reaction air pipe, a vortex synergistic reactor, an air equalizing device and a dust removal device which are sequentially arranged along the flue gas conveying direction;

the air equalizing device is communicated with the vortex synergistic reactor, a feeding pipeline of the material feeding device penetrates through a wall plate of the air equalizing device to extend to the upper side of the air equalizing device, and the initial deacidification agent and the flue gas containing the low-concentration acidic compound flowing out of the vortex synergistic reactor are subjected to primary reaction;

the dust removal device is arranged above the air equalizing device, a filter bag used for filtering particles is arranged on the dust removal device, a reaction ash layer which is attached to the particles and is driven by the rising of the flue gas is formed on the surface layer of the filter bag, so that in the process that the flue gas after primary reaction passes through the filter bag of the dust removal device, an acidic compound in the flue gas and a deacidification agent in the reaction ash layer are subjected to secondary reaction;

the material gasification bed is arranged below the air equalizing device, one end of the material circulation regulation and control device is connected with the material gasification bed, and the other end of the material circulation regulation and control device is connected to the reaction air pipe, so that the deacidification agent after the secondary reaction is conveyed into the reaction air pipe and is subjected to tertiary reaction with the initial flue gas;

the reaction air pipe is connected to the lower end of the vortex synergistic reactor, the flue gas and the deacidification agent passing through the reaction air pipe rise into the vortex synergistic reactor, and the flue gas and the deacidification agent are in full contact with the vortex synergistic reactor to carry out four times of reaction.

As a preferable scheme of the invention, a material distributing plate is arranged in the material gasification bed, the material distributing plate divides the interior of the material gasification bed into a circulation zone and a return zone, the material circulation regulating and controlling device is connected with the circulation zone of the material gasification bed, and the return zone of the material gasification bed is connected with an external return material conveying device.

In a preferred embodiment of the present invention, a gasification plate is disposed in the material gasification bed, and an external air flow flows into the material gasification bed through the gasification plate, wherein the gasification plate is made of a flexible woven material, and the gasification plate is capable of permeating gas and blocking powder particles.

As a preferable scheme of the present invention, the air equalizing device includes a housing, a second baffle, a third baffle, and a plurality of first baffles, the first baffle, the second baffle, and the third baffle are disposed in the housing, the plurality of first baffles are connected to the second baffle at intervals, a vertical channel is formed between two adjacent first baffles, one side of each first baffle, which is away from the second baffle, is connected to an upper side of an air outlet of the vortex synergistic reactor, and the third baffle is disposed on the housing opposite to the second baffle.

As a preferred embodiment of the present invention, the vortex effect-increasing reactor includes a housing and an outer arc plate, the outer arc plate and the housing form an effect-increasing chamber with a circular arc-shaped structure, a first vortex plate, a first guide plate, a second guide plate, a material homogenizing plate and a second vortex plate are disposed in the effect-increasing chamber, the first vortex plate, the first guide plate and the second guide plate are all arc-shaped structures, the first vortex plate is disposed at an inlet end, the first guide plate and the second guide plate are distributed in parallel and are both disposed opposite to the first vortex plate, the second vortex plate is disposed below the first guide plate and the second guide plate, and the material homogenizing plate is disposed at an outlet end.

As a preferred scheme of the present invention, a plurality of material diffusers are disposed in the reaction air duct, and the plurality of material diffusers are disposed along a duct wall of the reaction air duct; the tail end of the feeding pipeline of the material feeding device is provided with a material diffuser so as to uniformly distribute the deacidification agent in the air equalizing device.

As a preferable scheme of the invention, the device further comprises a supporting frame, the dust removal device is arranged on the upper side of the supporting frame, the air equalizing device is embedded in the supporting frame, the side part of the dust removal device is connected with an outlet flue, the lower end of the reaction air pipe is connected with an inlet flue, and valves are arranged on the inlet flue and the outlet flue.

Compared with the prior art, the invention has the following positive effects:

1. the invention provides a double-area cloth flue gas deacidification method which comprises the following steps: carrying out primary reaction on the initial deacidification agent and the flue gas containing the low-concentration acidic compound at the rear end of the flue gas path of the system; performing dust removal treatment on the flue gas subjected to the primary reaction so as to perform secondary reaction on the flue gas and a deacidification agent in the dust removal treatment process; returning the deacidification agent subjected to the secondary reaction to the front end of the flue gas path of the system and carrying out tertiary reaction with the initial flue gas; the deacidification agent after the three reactions and the smoke gas flow in a rotary mode, and the deacidification agent and the smoke gas are in full contact to carry out four reactions; wherein, the flue gas containing low-concentration acidic compounds in the first reaction is the flue gas after the fourth reaction. The flue gas deacidification method comprises the steps of primary reaction, secondary reaction, tertiary reaction and quartic reaction, so that an acidic compound in the flue gas and a deacidification agent are fully reacted, and the flue gas can be effectively purified; the fresh unreacted initial deacidification agent is firstly reacted with the flue gas containing the low-concentration acidic compound at the tail end of the flue gas path of the system, and then the deacidification agent after the secondary reaction is reacted with the initial flue gas containing the high-concentration acidic compound at the front end of the flue gas path of the system, so that the material is fed in a subarea manner, the deacidification agent is fully reacted with the flue gas, and the reaction process is more reasonable.

2. The invention provides a dual-zone distribution flue gas deacidification system which comprises a material gasification bed, a material circulation regulation and control device, a material feeding device, and a reaction air pipe, a vortex synergistic reactor, an air equalizing device and a dust removal device which are sequentially arranged along the flue gas conveying direction, wherein the dust removal device is arranged above the air equalizing device, the material gasification bed is arranged below the air equalizing device, the air equalizing device is connected with the vortex synergistic reactor, and the reaction air pipe is connected with the lower end of the vortex synergistic reactor. The flue gas flows through the reaction air pipe, the vortex synergistic reactor, the air equalizing device and the dust removal device in turn in the deacidification system, and the deacidification agent flows through the air equalizing device, the dust removal device, the reaction air pipe and the vortex synergistic reactor in turn in the deacidification system.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.

FIG. 1 is a process flow diagram of flue gas deacidification of the prior art;

FIG. 2 is a schematic diagram of a prior art material balance for flue gas deacidification;

FIG. 3 is a schematic process flow diagram of a flue gas deacidification process of the present invention;

FIG. 4 is a schematic illustration of the material balance of the flue gas deacidification process of the present invention;

FIG. 5 is a schematic illustration of the material balance for flue gas deacidification of the present invention;

FIG. 6 is a side view of the lower portion of the dust extraction module of the present invention;

FIG. 7 is a schematic diagram of the mechanism of the flue gas deacidification system of the present invention;

FIG. 8 is a three-dimensional view of the combination of the vortex booster reactor, the material gasification bed and the air-equalizing device in the present invention;

FIG. 9 is an isometric view of a vortex booster reactor of the present invention;

FIG. 10 is an isometric cross-sectional view of a vortex booster reactor of the present invention;

FIG. 11 is a side view of a vortex enhanced reactor of the present invention;

FIG. 12 is an isometric view of a reaction air duct of the present invention.

FIG. 13 is an axial cross-sectional view of a reaction air duct in the present invention.

In the figure: 1. a raw material bin; 2. a material feeding device; 21. a feeding pipeline; 3. a material circulation regulation and control device; 4. a reaction air duct; 41. a feeding port; 42. an outlet; 5. a vortex synergistic reactor; 51. a housing; 52. an outer arc plate; 53. a first whirl plate; 54. a second whirl plate; 55. a first baffle; 56. a second baffle; 57. A material homogenizing plate; 58. an air inlet; 59. an air outlet; 6. a wind equalizing device; 61. a first baffle plate; 62. a second baffle; 63. a third baffle plate; 64. a housing; 7. a dust removal device; 8. an outlet flue; 9. a feed back conveying device; 10. a material gasification bed; 101. a material distributing plate; 102. a return zone; 103. a circulation zone; 104. a gasification plate; 11. a product bin; 12. a smoke exhaust fan; 13. a material diffuser; 14. a chimney; 15. an inlet flue; 16. A tank car; 17. a support frame; 18. an overhaul shed.

Detailed Description

In the description of the present invention, it is to be noted that, unless otherwise specified, "a plurality" means two or more; the terms "upper", "lower", "front", "rear", "left", "right", "top", "bottom", "inner", "outer", "front", "rear", "head", "tail", and the like, indicate orientations or positional relationships that are based on the orientations or positional relationships shown in the drawings, are merely for convenience in describing and simplifying the present invention, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.

In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; may be directly connected or indirectly connected through an intermediate. The specific meaning of the above terms in the present invention can be understood as appropriate to those of ordinary skill in the art.

The following describes embodiments of the present invention in further detail with reference to the accompanying drawings.

Example 1

In the embodiment, as shown in fig. 3, the method for deacidifying flue gas in cloth in two regions includes the following steps:

carrying out primary reaction on the initial deacidification agent and the flue gas containing the low-concentration acidic compound at the rear end of the flue gas path of the system; wherein the initial deacidification agent is an unreacted deacidification agent.

Performing dust removal treatment on the flue gas subjected to the primary reaction so as to perform secondary reaction on the flue gas and a deacidification agent in the dust removal treatment process;

returning the deacidification agent subjected to the secondary reaction to the front end of the flue gas path of the system and carrying out a tertiary reaction with the initial flue gas; wherein the initial flue gas is fresh flue gas containing high-concentration acidic compounds.

Carrying out rotary flow on the deacidification agent after the three reactions and the flue gas to ensure that the deacidification agent and the flue gas are fully contacted to carry out four reactions; wherein, the flue gas containing the low-concentration acidic compound in the first reaction is the flue gas after the fourth reaction.

The flue gas deacidification method comprises a first reaction, a second reaction, a third reaction and a fourth reaction, so that the deacidification agent entering the system sequentially performs the first reaction, the second reaction, the third reaction and the fourth reaction, and the flue gas entering the system sequentially performs the third reaction, the fourth reaction, the first reaction and the second reaction. When the deacidification agent is fed, firstly, reacting a fresh unreacted initial deacidification agent with the flue gas containing the low-concentration acidic compound at the tail end of a flue gas path of a system to obtain a first-zone material distribution; then the deacidification agent after the secondary reaction after the reaction is reacted with the initial flue gas containing high-concentration acidic compounds at the front end of the flue gas path of the system, and the two-zone material distribution is obtained; therefore, the material feeding in a subarea mode is realized, the deacidification agent and the flue gas react more fully, the reaction process is more reasonable, the deacidification efficiency of the flue gas is improved, and the purification effect of the flue gas is better. Compared with the traditional mode of simultaneously putting primary materials and secondary materials into the front end of the flue gas path, the mode of distributing materials in a subarea mode does not need high wind speed material carrying, has low flue gas material carrying wind speed and small system pressure drop, reduces the load of the system material carrying, saves energy and reduces consumption. In addition, the flue gas effectively improves the purification effect of the flue gas after four times of absorption reactions, shortens the flue gas reaction path, reduces the equipment volume and reduces the equipment investment.

Preferably, the method of this embodiment further includes: conveying the deacidification agent which is subjected to the fourth reaction and is fully reacted out of the reaction system, carrying out dust removal treatment on one part of the deacidification agent which is not completely reacted under the driving of flue gas flow, and carrying out the third reaction on the other part of the deacidification agent which is subjected to the second reaction together with the deacidification agent which is subjected to the second reaction. And (4) leaving the deacidification agent which is not completely reacted in the system for circulating reaction until the deacidification agent is completely reacted and then discharging the deacidification agent out of the system. The deacidification agent can be fully reacted by recycling the deacidification agent, and the deacidification cost of the flue gas is reduced.

Preferably, the deacidification agent is Al₂O₃Powder or calcium-or sodium-based acid scavengers, Al₂O₃The specific surface area a of the powder satisfies that a is more than or equal to 35m²And/g, the mesh number b of the sodium-based acid scavenger particles meets the requirement that b is more than or equal to 500 meshes, and the calcium-based acid scavenger is quicklime or slaked lime. For the smoke containing fluorine compounds, Al is selected₂O₃The powder is used as a deacidification agent; for the flue gas containing sulfur compounds, a sodium-based acid scavenger is selected as an acid scavenger; for flue gas containing sulfur, fluorine and chlorine compounds, a calcium-based acid scavenger is selected as the acid scavenger. The deacidification agent material can flexibly deal with and treat the flue gas containing sulfur, fluorine and chlorine compounds according to the working condition of the flue gas.

Preferably, when the deacidification agent is a calcium-based deacidification agent, atomized water is added into the system, and the water content c of the calcium-based deacidification agent is enabled to meet c less than or equal to 5 percent. The atomized water is used as a reaction promoter, so that the calcium-based acid scavenger can better react with acidic compounds in the smoke.

The application tests the removal rate of the acid scavenger with different specific surfaces on the acidic compounds in the flue gas, and the specific steps are as follows:

the acid scavenger adopts common Al with different specific surface areas suitable for industrial batch purchase₂O₃And simulating smoke by using HF as an acid compound mixed gas. The results of comparison of the removal rates of acidic compounds are shown in Table 1.

Table 1:

it is seen from the comparison in Table 1 that the removal rate of the acidic compound and the fluorine-carrying rate of the reaction product show an increasing tendency with the increase of the surface area, when the specific surface area is 35m²In terms of/g, the fluorine-carrying rate of the reaction product is more than 0.3 percent, and the removal rate of the acidic compound is more than 90 percent.

The application performs experiments on the removal rate of acidic compounds in flue gas by the mesh number of different acid scavengers, and specifically comprises the following steps:

influence of sodium bicarbonate on removal rate of acidic compound in experiment, sodium-based acid scavenger is adopted as acid scavenger, namely sodium bicarbonate powder with different meshes is used, and SO is added₂The flue gas is simulated as the acid compound mixed gas.

In experimental working condition conditions: smoke temperature 80-130 ℃, SO₂Concentration 1000 mg/standard cubic meter, Na/s: 0.9-1.5, as shown in Table 2, the acid removal efficiency of sodium bicarbonate with different meshes was testedAnd (6) analyzing.

Table 2:

TABLE 3

The comparison in Table 3 shows that the difference in removal rates of acidic compounds is significant for baking soda powders of different mesh sizes when Na/S > 1. The difference in the number of the acid scavengers directly affects the removal rate of the acidic compounds. The dispersion speed of the deacidification agent powder is slow when the materials are just put into a system to participate in the addition reaction, the deacidification reaction is concentrated on the shell of the deacidification agent particles, and the deacidification reaction is concentrated in the particle interior and the gaps of the particle bodies along with the diffusion of the materials in the smoke.

This application has still been tested in the influence of the moisture content of different deacidification rates to flue gas acid compound desorption rate, specifically as follows:

in the experiment of the influence of the water content of the acid scavenger on the removal rate of the acid compound, the acid scavenger adopts a calcium-based acid scavenger, namely hydrated lime, and SO₂The flue gas is simulated as the acid compound mixed gas.

In experimental working condition conditions: smoke temperature 80-130 ℃, SO₂The concentration is 1000 mg/standard cubic meter, the water content of the acid scavenger is 1-6%, and the acid removal rate of the acid-removing acidic compound is experimentally analyzed as shown in table 4.

TABLE 4

TABLE 5

Water content%

1％

2％

3％

4％

5％

6％

Removal rate of acidic compound

35％

70％

88％

92％

97％

97.2％

The results of acid removal are shown in Table 5, and the comparison in Table 5 shows that the acid removal rate is directly affected by the acid remover. When the water content of the acid scavenger is increased, the removal rate of the acid compound is higher and higher, when the water content of the acid scavenger is more than or equal to 4%, the removal rate of the acid compound reaches more than 90%, and the water content is more preferably 4-5%. When the water content is more than 5 percent, the removal rate of the acidic compound is not changed greatly, and the excessive water content in the experimental process is not friendly to the transportation of materials and is easy to harden and deposit.

Example 2:

in this embodiment, a two-zone fabric flue gas deacidification system is provided, as shown in fig. 4 to 6, and the deacidification system is used for implementing the deacidification method in the present invention. The deacidification system comprises a material gasification bed 10, a material circulation regulating and controlling device 3, a material feeding device 2, a reaction air pipe 4, a vortex synergistic reactor 5, an air equalizing device 6 and a dust removing device 7 which are sequentially arranged along the flue gas conveying direction,

the air equalizing device 6 is communicated with the vortex synergistic reactor 5, the feeding pipeline 21 of the material feeding device 2 penetrates through a wall plate of the air equalizing device to extend to the upper side of the air equalizing device 6, and the initial deacidification agent and the flue gas containing the low-concentration acidic compound flowing out of the vortex synergistic reactor 5 are subjected to primary reaction. And conveying the initial deacidification agent to an air equalizing device to realize one-zone material distribution of the deacidification agent. The material feeding device 2 is arranged at the side part of the material gasification bed 10. A feed back conveying device 9 is arranged beside the material feeding device 2.

The dust removal device 7 is arranged above the air equalizing device 6, the dust removal device 7 is provided with a filter bag, a reaction ash layer which is attached by particles contained in the smoke gas and is driven by the rising of the smoke gas is formed on the surface layer of the filter bag, so that in the process that the smoke gas after primary reaction passes through the filter bag of the dust removal device, the acidic compounds in the smoke gas and the deacidification agent in the reaction ash layer carry out secondary reaction. Wherein, the particulate matters contained in the smoke comprise deacidification agents and dust carried by the smoke.

The material gasification bed 10 is arranged below the air equalizing device 6, one end of the material circulation regulation and control device 3 is connected with the material gasification bed 10, and the other end is connected with the reaction air pipe 4, so that the deacidification agent after the secondary reaction is conveyed into the reaction air pipe 4 and is subjected to a tertiary reaction with the initial flue gas containing high-concentration acidic compounds. And conveying the deacidification agent subjected to the secondary reaction to a reaction air pipe 4 to realize secondary distribution of the deacidification agent. The material circulation regulating and controlling device 3 is arranged in front of the reaction air pipe 4.

The reaction air pipe 4 is connected to the lower end of the vortex synergistic reactor 5, the flue gas and the deacidification agent which pass through the reaction air pipe 4 rise into the vortex synergistic reactor 5, and the flue gas and the deacidification agent are fully contacted in the vortex synergistic reactor 5 to carry out four times of reaction.

The flow path of the flue gas in the deacidification system in this embodiment is as follows: the reaction is carried out for three times in the reaction air pipe 4, the reaction is carried out for four times in the vortex synergistic reactor 5, at the moment, the flue gas becomes the flue gas containing low-concentration acidic compounds, then the flue gas is carried out for one time in the air equalizing device 6, then the secondary reaction is carried out through the dust removal device 7, and the flue gas after the reaction becomes clean gas and is discharged out of the atmosphere after entering the chimney 14 through the smoke exhaust fan 12.

The flow path of the acid scavenger in the deacidification system in this embodiment is: the fresh unreacted primary acid scavenger is fed into the air homogenizing device 6 through the material feeding device 2 (one-zone material distribution) to perform acid removal reaction with the smoke of the low-concentration acidic compound at the outlet of the vortex synergistic reactor 5, namely, the primary reaction. Under the action of negative pressure, the acid scavenger continuously rises along the air flow and is attached to the surface layer of the filter bag to form a reaction ash layer, and during the process that the flue gas passes through the filter bag, acid compounds in the flue gas and the acid scavenger in the reaction ash layer generate a deacidification reaction, namely a secondary reaction. Along with the thickening of the reaction ash layer, when the system resistance increases and reaches the design value, the dust removal device 7 starts to blow, the reaction ash layer is stripped from the surface of the filter bag and enters the material gasification bed 10, the material gasification bed 10 is connected with the material circulation regulation and control device 3, the effective components of the acid scavenger after the two-time deacidification reaction are reduced, and the acid scavenger after the second-time reaction is thrown into the reaction air pipe 4 (two-zone material distribution) through the material circulation regulation and control device 3 and is mixed with the high-concentration acidic compound flue gas to carry out the deacidification reaction, namely, the third-time reaction. The reaction air pipe 4 is connected with the vortex synergistic reactor 5, the air flow of the reaction air pipe 4 is mixed and then enters the vortex synergistic reactor 5 to carry out two processes of synergy and stripping, the air flow carries out convolution synergistic reaction in the vortex synergistic reactor 5, namely, four reactions, the reaction time is increased to promote the reaction to be more sufficient, and deacidification agents with different reaction degrees are separated.

The acid removal system disclosed by the invention can realize integration of acid removal and dust removal, is compact in structure, saves space, does not adopt a Venturi structure, does not have a reaction bed layer, does not have the risk of bed collapse of the traditional process technology, is low in system resistance, is stable in operation, can effectively purify flue gas, improves the deacidification efficiency, can enable the deacidification agent to be completely reacted, and enables the deacidification agent to be efficiently used.

Preferably, as shown in fig. 4 and 8, a material distributing plate 101 is arranged in the material gasification bed 10, the material distributing plate 101 divides the inside of the material gasification bed 10 into a circulation zone 103 and a return zone 102, the material circulation control device 3 is connected with the circulation zone 103 of the material gasification bed, and the return zone 102 of the material gasification bed is connected with the external feed back conveying device 9. The material gasification bed 10 is a box structure with an upward opening. The circulation zone 103 and the return zone 102 can separate the deacidification agent which is fully reacted from the deacidification agent which is incompletely reacted, thereby reducing the ineffective circulation of the deacidification agent and reducing the system load.

Preferably, a gasification plate 104 is arranged in the material gasification bed 10, external air flows into the material gasification bed through the gasification plate 104, the gasification plate 104 is made of a flexible woven material, and the gasification plate 104 is capable of permeating gas and blocking powder particles. The gasification plate 104 is disposed at the bottom of the material gasification bed 10. The material distribution plate 101 divides the inside of the material gasification bed 10 into a circulation zone 103 and a return zone 102 on the gasification plate 104, and an external air flow flows to the circulation zone 103 and the return zone 102 of the material gasification bed through the gasification plate 104. The gas source of the material gasification bed 10 is from a gas supply fan or compressed air, which enters the bed zone through the gasification plate 104, and the air mixes with the material in the bed zone to make the material in a fluidized state.

Preferably, as shown in fig. 9-11, the vortex synergistic reactor 5 includes a housing 51 and an outer arc plate 52, the outer arc plate 52 and the housing 51 are combined to form a synergistic chamber with a circular arc arch structure, a first vortex plate 53, a first guide plate 55, a second guide plate 56, a refining plate 57 and a second vortex plate 54 are disposed in the synergistic chamber, the first vortex plate 53, the first guide plate 55 and the second guide plate 56 are all arc structures, the first vortex plate 53 is disposed at an inlet end, the first guide plate 55 and the second guide plate 56 are distributed in parallel and are both disposed opposite to the first vortex plate 53, the second vortex plate 54 is disposed below the first guide plate 55 and the second guide plate 56, and the refining plate 57 is disposed at an outlet end. The upper lateral swirl enhancing reactor 5 of the second swirl plate 54 is curved in an arc shape. The air inlet 58 of the vortex synergistic reactor 5 is arranged at the lower part of the shell 51, and the air outlet 59 is arranged at the side part of the shell 51.

The deacidification agent enters the vortex synergistic reactor 5 from the air inlet 58 to carry out synergy and stripping, wherein the synergy process comprises the following steps: the deacidification agent carries out the convolution synergistic reaction in the vortex synergistic reactor 5 by utilizing the principle of a Tesla valve, increases the reaction residence time of the deacidification agent and promotes the reaction to be more sufficient; and (3) stripping process: the centrifugal force of the substances which are relatively fully reacted is large, the substances enter the return area 102 of the material gasification bed from the air outlet 59 and are discharged outside the second guide plate 56 and the refining plate 57, and the substances are conveyed to the product bin 11 through the material return conveying device 9 and conveyed through the tank car 16; the centrifugal force of substances which are not completely reacted is small, one part of the substances enters the circulation area 103 of the material gasification bed from the air outlet 59 along the inner sides of the first guide plate 55 and the second guide plate 56 for recirculation, and the other part of the substances enters the dust removal device 7 along with the air flow and is attached to the surface of the filter bag through the air equalizing device 6 to form a reaction ash layer.

The first guide plate 55 and the second guide plate 56 serve to guide flow and reduce resistance, and the end parts of the first guide plate and the second guide plate can destroy the reacted solidified shell of the deacidification powder, expose the part which does not participate in the reaction, improve the utilization rate of the deacidification powder, and further can serve to distinguish material attributes and distinguish completely reacted materials from incompletely reacted materials. The first vortex plate 53 and the second vortex plate 54 can increase the retention time of flue gas, increase the reaction duration, improve the circulation rate, shorten the reaction path, reduce the occupied space of equipment, and the equipment modular design is compact in layout, and the problems of long reaction path and large equipment volume of the traditional deacidification technology are solved.

The material gasification bed return zone 102 is close to the outer sides of the second guide plate 56 and the material homogenizing plate 57, and the material gasification bed circulation zone 103 is close to the inner sides of the first guide plate 55 and the second guide plate 56, so that the deacidification agent with more sufficient reaction enters the return zone 102, and the deacidification agent with incomplete reaction enters the circulation zone 103.

Preferably, as shown in fig. 8, the air equalizing device 6 includes a housing 64, a second baffle plate 62, a third baffle plate 63, and a plurality of first baffle plates 61, the first baffle plate 61, the second baffle plate 62, and the third baffle plate 63 are disposed in the housing 64, the plurality of first baffle plates 61 are connected to the second baffle plate 62 at intervals, a vertical channel is formed between two adjacent first baffle plates 61, one side of the first baffle plate 61 facing away from the second baffle plate 62 is connected to the upper side of the air outlet 59 of the swirl-enhanced reactor 5, and the third baffle plate 63 is disposed on the housing 64 opposite to the second baffle plate 62. The upper end of the second baffle plate 62 is bent toward the swirl enhancement reactor 5 side, and the upper end of the third baffle plate 63 is bent toward the side away from the second baffle plate 62. The bottom end of the air equalizing device 6 is connected with the upper end of the material gasification bed 10. The airflow from the air outlet 59 of the vortex synergistic reactor 5 is obtained by transverse flow, and the vortex synergistic reactor 5 can integrate the airflow and change the airflow direction, so that the airflow rises and is distributed to the dust removing device 7 in a balanced manner.

The vortex synergistic reactor 5, the material gasification bed 10 and the air equalizing device 6 are combined, airflow carries out convolution synergistic reaction in the vortex synergistic reactor 5 by adopting the principle of a Tesla valve, and the reaction time is increased to promote the reaction to be more sufficient. The incompletely reacted materials in the vortex synergistic reactor 5 enter the material gasification bed circulation zone 103 for continuous use, and the completely reacted materials enter the material gasification bed return zone 102 and are discharged. Compared with the prior art, the method has the advantages that substances which are completely reacted and incompletely reacted are separated, so that ineffective circulation of the materials can be reduced, the proportion of raw material components in reaction products is reduced, the burden of a rear dust removal device is reduced due to material separation, the abrasion of a filter bag is reduced, the efficient use of the materials is realized, and the energy is saved and the consumption is reduced.

Preferably, as shown in fig. 12 and 13, a plurality of material diffusers 13 are disposed in the reaction air duct 4, the plurality of material diffusers 13 are disposed along the wall of the reaction air duct 4, and the secondary deacidification agent is rapidly mixed with the flue gas containing high-concentration acidic compounds under the action of the material diffusers 13 to perform the deacidification reaction. The tube wall of the reaction air duct 4 is provided with a plurality of material inlet openings 41, the material inlet openings 41 are connected with the material circulation control device 3, the material diffuser 13 is arranged in the reaction air duct 4 on the opposite side of the material inlet openings 41 corresponding to the material inlet openings 41, so that the secondary deacidification agent conveyed to the position of the material inlet opening 41 of the reaction air duct by the material circulation control device 3 is uniformly dispersed. The air channel of the reaction air pipe 4 is vertically arranged, the outlet 42 is arranged at the upper end of the reaction air pipe 4, and the reaction air pipe 4 is connected with the air inlet 58 of the vortex synergistic reactor 5 through the outlet 42.

The end of the feeding pipeline 21 of the material feeding device 2 is provided with a material diffuser to uniformly distribute the deacidification agent in the air equalizing device 6. The tail end of the dense phase pipeline is provided with a material diffuser, materials are uniformly distributed in the air homogenizing device 6 under the action of the material diffuser, a reaction ash layer is uniformly attached to the surface of a filter bag of the dust removal device 7 under the driving of air homogenizing airflow, and the combination of the reaction ash layer and the filter bag is equivalent to a fixed bed type reactor, so that the reaction effect is enhanced. Wherein the material diffuser may be a fan, as shown in fig. 12.

Preferably, as shown in fig. 6 and 7, the deacidification system of this embodiment further includes a supporting frame 17, the dust removing device 7 is disposed on the upper side of the supporting frame 17, the air equalizing device 6 is embedded in the supporting frame 17, the side of the dust removing device 7 is connected with the outlet flue 8, the lower end of the reaction air duct 4 is connected with the inlet flue 15, the inlet flue 15 and the outlet flue 8 are respectively provided with a valve, so that multiple modules in the system can be put into operation or switched, and one module is stopped for maintenance without affecting the operation of other modules. A plurality of dust removing device 7 modules are arranged on the supporting frame 17 in a row, and an overhaul shed 18 with a rainproof overhaul function is arranged on the dust removing device 7 modules.

The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can make several variations and modifications without departing from the inventive concept of the present invention, and all such variations and modifications are intended to be covered by the present invention.