Device and method for improving calcium-based dry desulfurization efficiency by utilizing fluid self-oscillation

Abstract

The invention belongs to the technical field of flue gas purification, and relates to a device and a method for improving calcium-based dry desulfurization efficiency by utilizing fluid self-oscillation, the device comprises a fluid self-oscillation device connected between a powdery desulfurization catalyst conveying pipeline and a desulfurization reactor; the fluid self-oscillation device comprises a fluid mixing cavity and a fluid feedback channel, a fluid inlet section is arranged at one end, close to the powdery desulfurization catalyst conveying pipeline, of the fluid mixing cavity, a fluid outlet section and an outflow diverging section are sequentially arranged at one end, close to the desulfurization reactor, of the fluid mixing cavity, and the fluid self-oscillation device is connected with the desulfurization reactor through the outflow diverging section; one end of the fluid feedback channel is connected to the fluid inlet section of the fluid mixing cavity, and the other end of the fluid feedback channel is connected to the fluid outlet section of the fluid mixing cavity. The fluid self-oscillation device with a special structure is used for spraying the powdery desulfurization catalyst, so that the aim of improving the calcium-based dry desulfurization efficiency is fulfilled.

Description

Technical Field

[0001] The invention belongs to the technical field of flue gas purification, and relates to a device and a method for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation. Background Art

[0002] To meet the national requirements for ultra-low emission of flue gas SO2 (<35mg / Nm 3 ) requirements, calcium-based dry desulfurization technology is currently used. However, the existing calcium-based dry desulfurization technology has the following problems: (1) The actual Ca(OH)2 desulfurizer is easy to absorb moisture and agglomerate, which hinders the diffusion of SO2 inside the desulfurizer and leads to low desulfurizer utilization rate; (2) The actual desulfurization reactor is mostly a flue gas duct. After the desulfurizer is sprayed into the flue gas duct, it is quickly carried away by the flue gas, and the desulfurizer residence time is short; (3) In actual operation, the desulfurizer that absorbs moisture and agglomerates easily blocks the injection port; (4) At present, the efficiency of calcium-based dry desulfurization is only about 70%, and the actual Ca / S ratio is about 4 to 5, and a large amount of Ca(OH)2 is wasted.

[0003] In order to solve the above problems, the industry is currently focusing on the preparation of highly active and multifunctional calcium-based desulfurizers. There is little research on how to strengthen the reaction process of Ca(OH)2 and SO2, as well as the desulfurizer moisture absorption and agglomeration, short desulfurizer residence time, and fluctuating SO2 concentration in flue gas in actual field applications. Although in the prior art, the powdered desulfurizer injection port can be evenly arranged in other fields to improve the contact and mixing of the desulfurizer and SO2 in the flue gas. However, in actual operation, due to the moisture absorption and agglomeration of the desulfurizer, the injection port is easily blocked, the effect is minimal, and the flue gas flow resistance is increased.

[0004] Therefore, how to increase the desulfurization time of powdered desulfurizer in the desulfurization reactor, improve the mixed contact between the desulfurizer and SO2 in the flue gas, and solve the problems of insufficient catalyst utilization caused by the actual desulfurizer's easy moisture absorption and agglomeration are the core of improving the efficiency of calcium-based dry desulfurization. Summary of the invention

[0005] In view of this, the purpose of the present invention is to provide a device and method for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation, and to provide a fluid self-oscillation device with a special structure for spraying powdered desulfurization catalyst, so that after the powdered desulfurization catalyst passes through the fluid self-oscillation device, a periodic sweeping oscillating fluid is formed in the outflow expansion section of the fluid self-oscillation device, and it reacts with the flue gas in the desulfurization reactor to form secondary reflux and secondary vortex, thereby improving the mixed contact between the powdered desulfurizer and SO2 in the flue gas, increasing the residence time of the desulfurizer, breaking up the agglomerated desulfurizer, and separating the CaSO4 solid oscillation generated by the reaction of the desulfurizer and SO2 and covering the surface of the desulfurizer, thereby improving the exposure of the unreacted desulfurizer inside, so as to achieve the purpose of improving the efficiency of calcium-based dry desulfurization.

[0006] In order to achieve the above object, the present invention provides the following technical solutions:

[0007] A device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation, comprising a powdered desulfurization catalyst delivery pipeline and a desulfurization reactor, and also comprising a fluid self-oscillation device connected between the powdered desulfurization catalyst delivery pipeline and the desulfurization reactor;

[0008] The fluid self-oscillation device comprises a fluid mixing chamber and a fluid feedback channel, the two ends of the fluid mixing chamber are respectively connected to the powdered desulfurization catalyst delivery pipeline and the desulfurization reactor, and a fluid inlet section is provided at one end of the fluid mixing chamber close to the powdered desulfurization catalyst delivery pipeline, and a fluid outlet section and an outflow gradually expanding section are sequentially provided at one end of the fluid mixing chamber close to the desulfurization reactor, and the large end of the outflow gradually expanding section is connected to the desulfurization reactor;

[0009] One end of the fluid feedback channel is connected to the side of the fluid inlet section on the fluid mixing chamber close to the powdered desulfurization catalyst delivery pipeline, and the other end of the fluid feedback channel is connected to the side of the fluid outlet section on the fluid mixing chamber close to the desulfurization reactor, so as to form a feedback flow in the fluid mixing chamber from the fluid outlet section to the powdered desulfurization catalyst delivery pipeline and the fluid inlet section.

[0010] Furthermore, the fluid self-oscillation device comprises a shell and a flow-dividing island which is suspended in an annular manner in the inner cavity of the shell, wherein the flow-dividing island and the shell are both hollow shells with two ends connected, so as to form a fluid mixing chamber in the inner cavity of the flow-dividing island, and an annular channel connecting the two ends of the fluid mixing chamber is formed between the flow-dividing island and the shell to serve as a fluid feedback channel;

[0011] The shell has an inlet connected to the powdered desulfurization catalyst delivery pipeline and an outlet connected to the desulfurization reactor, and a fluid outlet section and an outflow expansion section are provided at the outlet of the shell, and the end of the diverter island close to the shell inlet is set as the fluid inlet section, and the inlet, fluid inlet section, fluid outlet section and outflow expansion section of the shell are coaxially arranged.

[0012] Further, the size H1 of the housing inlet is 50-2000 mm, and the relationship between the size H2 of the fluid inlet section and H1 is H1:H2=1:1-2;

[0013] The relationship between the circumferential dimension H3 of the fluid mixing chamber and H1 is H1:H3=1:2-6, the relationship between the length dimension L3 of the fluid mixing chamber and H1 is H1:L3=1:1.5-6, and the mixing chamber expansion angle α of the hole section connecting the fluid mixing chamber to the fluid inlet section is 110-170°;

[0014] The relationship between the shell length dimension L2 and H1 is H1:L2=1:6~12, and the relationship between the shell circumferential dimension H4 and H1 is H1:H4=1:5~15;

[0015] The relationship between the fluid outlet section dimensions H5 and H1 is H1:H5=1:1~2, the relationship between the fluid outlet gradually expanding section large diameter end dimensions H6 and H1 is H1:H6=1:6~10, and the fluid outlet gradually expanding section opening angle β is 90~170°;

[0016] The relationship between the fluid feedback channel dimensions H7 and H1 is H1:H7=1:1~2.5, and the relationship between the fluid feedback channel outlet dimensions L1 and H1 is H1:L1=1:1~1.5.

[0017] Furthermore, a plurality of active ejectors are arranged evenly spaced along the circumferential direction and the wall profile direction on the inner wall of the fluid mixing chamber to eject jet gas into the fluid mixing chamber.

[0018] Furthermore, the active injector is connected to a fluid supply facility that provides jet gas to the active injector, and the fluid supply facility is connected to a control system. The control system is also connected to a CEMS system that is respectively arranged at the flue gas inlet and the flue gas outlet of the desulfurization reactor, so that the control system can dynamically adjust the fluid supply facility according to the monitoring data of the CEMS system, and thereby dynamically adjust the jet gas of the active injector.

[0019] Furthermore, the distance between the active ejector and the fluid inlet section is D1, and D1:L3=0.2~0.3, and the angle between the central axis of the active ejector and the corresponding wall profile at its installation position on the inner wall of the fluid mixing chamber is -10~10°.

[0020] Furthermore, the injection head of the active injector is a multi-fluid nozzle, and the diameter of the droplets sprayed by the multi-fluid nozzle is not greater than 50 microns.

[0021] Furthermore, a plurality of flow spoilers are arranged at intervals along the circumferential direction and the wall profile direction on the inner wall of the fluid mixing chamber to form a turbulent flow in the fluid mixing chamber.

[0022] Furthermore, the distance between the flow spoiler and the fluid inlet section is D2, and D2:L3=0.45-0.8, and the angle between the central axis of the flow spoiler and the corresponding wall profile at its installation position on the inner wall of the fluid mixing chamber is -4-12°.

[0023] Further, the fluid self-oscillation device comprises a fluid mixing housing and at least two fluid feedback pipes arranged in parallel outside the fluid mixing housing;

[0024] The fluid mixing shell is a hollow shell with two ends connected to form a fluid mixing chamber in the inner cavity of the fluid mixing shell. One end of the fluid mixing shell is an inlet connected to the powdered desulfurization catalyst delivery pipeline, and the other end is an outlet connected to the desulfurization reactor. A fluid inlet section is provided at the inlet of the fluid mixing shell, and a fluid outlet section and an outflow expansion section arranged along the flow direction of the powdered desulfurization catalyst are provided at the outlet. One end of the fluid feedback pipeline is connected to the side of the inlet of the fluid mixing shell close to the powdered desulfurization catalyst delivery pipeline, and the other end is connected to the outlet of the fluid mixing shell close to the fluid outlet section.

[0025] On the other hand, the present invention also provides a method for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation, and the device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation specifically comprises the following steps:

[0026] Step 1. The powdered desulfurization catalyst in the powdered desulfurization catalyst delivery pipeline is sprayed into the fluid self-oscillation device under the action of a fan, and then sprayed into the desulfurization reactor after forming a periodic sweeping and swinging fluid in the outflow expansion section of the fluid self-oscillation device to form a desulfurization reaction zone, and a secondary vortex is formed by the periodic sweeping and swinging fluid and the flue gas in the desulfurization reactor to increase the mixing contact and residence time of the powdered desulfurizer and the flue gas.

[0027] Further, it also includes step 2,

[0028] Step 2: After the powdered desulfurization catalyst reacts with the flue gas in the desulfurization reactor, the desulfurized flue gas is transported to a dust collector for dust removal to obtain clean flue gas, and then the clean flue gas is discharged into the atmosphere through a chimney.

[0029] Further, the period of the periodic sweeping oscillating fluid is T;

[0030] At time t=0T, the mainstream direction of the periodically sweeping and oscillating fluid is close to the upstream of the smoke, and interacts with the smoke to form a secondary vortex close to the downstream of the smoke;

[0031] At time t=1 / 4T, the mainstream direction of the periodically swept oscillating fluid is in the middle of the outflow expansion section, and reacts with the smoke to form a new secondary vortex close to the upstream of the smoke, while the tail vortex formed by the secondary vortex at time t=0T is close to the downstream of the smoke;

[0032] At time t=1 / 2T, the mainstream direction of the periodically sweeping and oscillating fluid is close to the downstream of the smoke, and interacts with the smoke to form a secondary vortex close to the upstream of the smoke;

[0033] At time t=3 / 4T, the mainstream direction of the periodically swept oscillating fluid is in the middle of the outflow expansion section, and interacts with the smoke to form a new secondary vortex close to the upstream of the smoke. At the same time, the tail vortex formed by the secondary vortex at t=1 / 2T is close to the downstream of the smoke.

[0034] Further, jet gas is injected into the fluid mixing chamber through a plurality of active injectors evenly spaced along the circumferential direction on the inner wall of the fluid mixing chamber;

[0035] The active ejector is connected to a fluid supply facility that provides jet gas to the active ejector, and the fluid supply facility is connected to a control system. The control system is also connected to a CEMS system that is respectively arranged at the flue gas inlet and the chimney outlet in the desulfurization reactor, so that the control system can dynamically adjust the fluid supply facility according to the monitoring data of the CEMS system, and then dynamically adjust the jet gas of the active ejector, and then actively regulate the period T, frequency v and sweeping angle of the periodic sweeping oscillating fluid formed by the fluid self-oscillation device.

[0036] Furthermore, the jet gas is a combination of one or more of air, flue gas and nitrogen.

[0037] Furthermore, the temperature of the desulfurization reaction zone is controlled between 50°C and 350°C, the powdered desulfurization catalyst is a calcium-based desulfurizer, preferably Ca(OH)2, and the flue gas has a SO2 concentration of less than 400 mg / Nm 3 of smoke.

[0038] The beneficial effects of the present invention are:

[0039] First, the present invention realizes efficient injection and dispersion of powdered desulfurizer through a fluid self-oscillation device. The device uses a special fluid dynamics design to form a periodic sweeping oscillating fluid from the highly viscous powdered desulfurizer during the injection process. This flow characteristic interacts with the flue gas in the desulfurization reactor to form a secondary vortex. This innovative design not only significantly increases the residence time of the desulfurizer in the reactor, but also enhances the mixed contact between the desulfurizer and SO2 in the flue gas, making the desulfurization reaction more complete. At the same time, the fluid self-oscillation device can also effectively break up the agglomerated desulfurizer and expose the unreacted desulfurizer inside, thereby greatly improving the efficiency of calcium-based dry desulfurization from the traditional 70% to 95%.

[0040] Secondly, the present invention has achieved significant environmental and economic benefits in practical applications. By using the method of the present invention, the SO2 concentration in the flue gas can be reduced from 400 mg / Nm 3 Reduced to 20mg / Nm 3 , far below the national ultra-low emission standard (<35mg / Nm 3 ). This breakthrough not only meets environmental protection requirements, but also greatly improves the utilization efficiency of desulfurizers. In fact, the application of the present invention reduces the actual Ca / S ratio of calcium-based dry desulfurizers from 4 to about 2.5, which means that the amount of desulfurizer required is greatly reduced to achieve the same desulfurization effect, thereby reducing the cost of flue gas desulfurization.

[0041] Finally, the fluid self-oscillation device of the present invention has many advantages in design. It avoids the cavitation phenomenon of traditional direct injection nozzles, has a higher flow coefficient and lower fan power requirements. Although vortices are generated during the injection process, the flow resistance is not significantly increased. In addition, the device can effectively avoid the problem of powdered desulfurizer clogging the injection port, and the active ejector is used as a temporary gas volume supplement, completely eliminating the cost of installing an additional fan. These design optimizations not only improve the reliability and stability of the device, but also further improve its economy and feasibility in practical applications.

[0042] Other advantages, objectives and features of the present invention will be described in the following description to some extent, and to some extent, will be obvious to those skilled in the art based on the following examination and study, or can be taught from the practice of the present invention. The objectives and other advantages of the present invention can be realized and obtained through the following description. BRIEF DESCRIPTION OF THE DRAWINGS

[0043] In order to make the purpose, technical solutions and advantages of the present invention more clear, the present invention will be described in detail below in conjunction with the accompanying drawings, wherein:

[0044] Figure 1Schematic diagram of the structure of the fluid self-oscillation device in Example 1;

[0045] Figure 2 Schematic diagram of the flow mixing process at t=0T in Example 1;

[0046] Figure 3 Schematic diagram of the flow mixing process at t=1 / 4T in Example 1;

[0047] Figure 4 Schematic diagram of the flow mixing process at t=1 / 2T in Example 1;

[0048] Figure 5 Schematic diagram of the flow mixing process at t=3 / 4T in Example 1;

[0049] Figure 6 It is a schematic diagram of the three-dimensional structure of the fluid self-oscillation device in Example 1;

[0050] Figure 7 Schematic diagram of structural parameters of the fluid self-oscillation device in Example 2;

[0051] Figure 8 Schematic diagram of the function of the active ejector and the spoiler in the embodiment;

[0052] Fig. 9 is a schematic diagram of the structure of the active ejector in Example 3;

[0053] Fig.10 is a schematic structural diagram of a flow spoiler in Example 4;

[0054] Fig.11 This is a flow field diagram of directly injecting powdered desulfurization catalyst through a powdered desulfurization catalyst delivery pipeline in the prior art;

[0055] Fig.12 This is a flow field diagram of spraying powdered desulfurization catalyst through a fluid self-oscillation device in an embodiment;

[0056] Fig.13 is a schematic diagram of the three-dimensional structure of the fluid self-oscillation device in Example 5;

[0057] Fig.14 It is a schematic diagram of the three-dimensional structure of the fluid self-oscillation device in Example 6.

[0058] Figure numerals: 1-powdered desulfurization catalyst; 2-housing; 3-fluid inlet section; 4-fluid feedback channel; 5-diverter island; 6-active ejector; 7-flow spoiler; 8-fluid mixing chamber; 9-fluid outlet section; 10-outflow expansion section; 11-outflow direction of powdered desulfurization catalyst; 12-t 0TTime fluid mixing chamber vortex; 13-oscillation flow boundary; 14-t 0T Time oscillation main flow; 15-t 0T Secondary vortex generated by momentary oscillating flow and flue gas; 16-flue gas; 17-desulfurized flue gas; 18-feedback flow; 19-t 0T Main stream of momentary feedback flow; 20-t 1 / 4T Main stream of constant feedback flow; 21-t 1 / 4T The main flow of the feedback flow and the secondary vortex of the powdered desulfurization catalyst; 22-t 1 / 4T Main vortex of fluid mixing chamber at time 23-t 1 / 4T Time oscillation flow mainstream; 24-t 1 / 4T Secondary vortex generated by momentary oscillating flow and smoke; 25-t 0T Time oscillating flow and smoke tail vortex; 26-t 1 / 2T Main stream of constant feedback flow; 27-t 1 / 2T Time fluid mixing chamber vortex; 28-t 1 / 2T Time oscillation flow mainstream; 29-t 1 / 2T Secondary vortex generated by momentary feedback flow and flue gas; 30-t 3 / 4T Always give feedback to the mainstream; 31-t 3 / 4T Constant feedback of the mainstream and the secondary vortex of the powdered desulfurization catalyst; 32-t 3 / 4T Main vortex of fluid mixing chamber at time 33-t 3 / 4T Time oscillation flow mainstream; 34-t 3 / 4T Secondary vortex generated by momentary oscillating flow and smoke; 35-t 1 / 2T The momentary oscillating flow and the tail vortex of flue gas; 36-shell inlet size H1; 37-fluid inlet section size H2; 38-fluid mixing chamber circumferential size H3; 39-shell circumferential size H4; 40-fluid outlet section size H5; 41-fluid outflow gradually expanding section large diameter end size H6; 42-fluid feedback channel outlet size L1; 43-shell length size L2; 44-fluid outflow gradually expanding section opening angle β; 45-fluid mixing chamber length size L3; 46-mixing chamber expansion angle α; 47-fluid feedback channel size H7; 48-oscillating flow periodic oscillation curve; 49-fluid self-oscillation device; 50-powdered desulfurization Catalyst delivery pipeline; 51-desulfurization reactor; 500-fluid mixing shell; 510-fluid feedback pipeline; 511-fluid feedback combined pipeline; 61-active ejector jet tail flow; 62-active ejector front end inlet; 63-active ejector inclined surface; 64-active ejector tail injection port; 71-flow spoiler disturbed tail flow; 72-flow spoiler inclination angle; 73-flow spoiler top structure; 74-flow spoiler tail structure; 75-arrangement angle of adjacent flow spoilers; 76-the distance between the active ejector and the fluid inlet section is D1; ​​77-the distance between the flow spoiler and the fluid inlet section is D2. DETAILED DESCRIPTION

[0059] The following describes the embodiments of the present invention by specific examples, and those skilled in the art can easily understand other advantages and effects of the present invention from the contents disclosed in this specification. The present invention can also be implemented or applied through other different specific embodiments, and the details in this specification can also be modified or changed in various ways based on different viewpoints and applications without departing from the spirit of the present invention. It should be noted that the illustrations provided in the following embodiments only illustrate the basic concept of the present invention in a schematic manner, and the following embodiments and features in the embodiments can be combined with each other without conflict.

[0060] Among them, the drawings are only used for illustrative explanations, and they only represent schematic diagrams rather than actual pictures, and should not be understood as limitations on the present invention. In order to better illustrate the embodiments of the present invention, some parts of the drawings may be omitted, enlarged or reduced, and do not represent the size of actual products. For those skilled in the art, it is understandable that some well-known structures and their descriptions in the drawings may be omitted.

[0061] The same or similar numbers in the drawings of the embodiments of the present invention correspond to the same or similar parts; in the description of the present invention, it should be understood that if the terms "upper", "lower", "left", "right", "front", "rear", etc. indicate the orientation or position relationship, they are based on the orientation or position relationship shown in the drawings, which is only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operate in a specific orientation. Therefore, the terms describing the position relationship in the drawings are only used for illustrative purposes and cannot be understood as limiting the present invention. For ordinary technicians in this field, the specific meanings of the above terms can be understood according to specific circumstances.

[0062] Example 1

[0063] See also Figure 1 to Figure 6 , is a device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation, comprising a fluid self-oscillation device 49 arranged between a powdered desulfurization catalyst delivery pipeline 50 and a desulfurization reactor 51, wherein the powdered desulfurization catalyst delivery pipeline 50 is connected to the inlet of the fluid self-oscillation device 49, and the powdered desulfurization catalyst 1 is sprayed into the fluid self-oscillation device 49 under the action of a fan, and the outlet of the fluid self-oscillation device 49 is connected to the desulfurization reactor 51, and a periodic sweeping oscillating fluid is formed at the outlet of the fluid self-oscillation device 49, and then the powdered desulfurization catalyst is sprayed into the desulfurization reactor in the form of periodic oscillation;

[0064] The fluid self-oscillation device 49 includes a shell 2 and a flow-dividing island 5 (i.e., a fluid mixing shell) that is suspended in an annular shape in the inner cavity of the shell 2. The flow-dividing island 5 and the shell 2 are both hollow shells with two ends connected, so as to form a fluid mixing chamber 8 in the inner cavity of the flow-dividing island 5. An annular channel connecting the two ends of the fluid mixing chamber is formed between the flow-dividing island 5 and the shell 2 to serve as a fluid feedback channel 4, and the two ends of the fluid feedback channel 4 are respectively arranged on the outer sides of the two ends of the flow-dividing island 5.

[0065] Specifically, a connecting rod for supporting the diverter island 5 is provided between the shell 2 and the diverter island 5 , so that the diverter island 5 can be arranged in an annular suspended manner in the inner cavity of the shell 2 .

[0066] The shell 2 has an inlet connected to the powdered desulfurization catalyst delivery pipeline 50 and an outlet connected to the desulfurization reactor 51, and a fluid outlet section 9 and an outflow expansion section 10 are provided at the outlet of the shell 2, and the end of the diverter island 5 close to the inlet of the shell 2 is set as the fluid inlet section 3, and the inlet, fluid inlet section 3, fluid outlet section 9 and outflow expansion section 10 of the shell 2 are coaxially arranged, and the two ends of the fluid feedback channel 4 are respectively connected to the fluid inlet section 3 and the fluid outlet section 9, and the end of the fluid feedback channel 4 connected to the fluid inlet section 3 is arranged on the side of the fluid inlet section 3 close to the powdered desulfurization catalyst delivery pipeline 50.

[0067] Under the action of the fan, the highly viscous powdered desulfurization catalyst 1 flows into the fluid mixing chamber 8 through the inlet of the casing 2 and the fluid inlet section 3, and forms a vortex in the fluid mixing chamber 8. Then, the mainstream of the vortex passes through the fluid outlet section 9 and the outflow expansion section 10, and flows into the desulfurization reactor 51 from the outflow direction 11 of the powdered desulfurization catalyst, carrying the powdered desulfurization catalyst 1, and reacts with the flue gas 16 to form a secondary vortex. Under the flow limiting action of the fluid outlet section 9, part of the vortex fluid forms a feedback flow 18 through the fluid feedback channel 4 and flows back to the fluid inlet section 3. Subsequently, a new vortex is generated in the fluid mixing chamber 8, pushing the powdered desulfurization catalyst to swing to the other side. As the direction of the mainstream of the feedback flow changes and the powdered desulfurization catalyst continues to act, the powdered desulfurization catalyst forms a sweeping swing with a period T within the range of the oscillation flow boundary 13 (sweep angle) in the outflow expansion section 10 of the fluid self-oscillation device without the action of active control components.

[0068] See also Figure 2 to Figure 5 , using the above scheme, the powdered desulfurization catalyst enters the fluid self-oscillation device, and the period of its periodic sweeping oscillating fluid is as follows:

[0069] At time t=0T, the powdered desulfurization catalyst flows into the fluid mixing chamber 8 through the inlet of the housing 2 and the fluid inlet section 3, and forms t 0TAt time t, the fluid mixing chamber vortex 12, and then t 0T At time t, the mainstream of the fluid mixing chamber vortex flows through the fluid outlet section 9 and the outflow expansion section 10 from the outflow direction 11 of the powdered desulfurization catalyst and flows into the desulfurization reactor 51 with the powdered desulfurization catalyst. At this time, the periodic sweeping oscillating fluid formed by the fluid self-oscillation device is t 0T The oscillating flow main stream 14 at the moment is close to the incoming flow direction of the flue gas 16 (upstream of the flue gas), so that t 0T At the moment, the oscillating flow main stream 14 and the flue gas 16 interact to form a t near the downstream of the flue gas. 0T The oscillating flow and the smoke generate a secondary vortex 15, and part of t 0T At the moment, the fluid mixing chamber vortex 12 forms a t on the downstream side close to the flow direction of the smoke 16 through the fluid feedback channel 4 under the flow limiting effect of the fluid outlet section 9. 0T The feedback flow 18 dominated by the main feedback flow 19 at the moment flows back to the fluid inlet section 3;

[0070] At time t=1 / 4T, the t 0T At time t, the main flow 19 of the feedback flow returns from the fluid feedback channel 4 to the fluid inlet section 3 to form 1 / 4T The main flow 20 is fed back at all times and merges with the powdered desulfurization catalyst 1 at the fluid inlet section 3. The powdered desulfurization catalyst 1 is t 1 / 4T The main flow 20 of the feedback flow is generated in the fluid mixing chamber 8 at a certain time. 1 / 4T The main flow of the moment feedback flow and the secondary vortex 21 and t 1 / 4T At the moment the main vortex 22 of the fluid mixing chamber, and the t 1 / 4T The secondary vortex 21 of the main flow of the feedback flow and the powdered desulfurization catalyst is close to the downstream side of the flow direction of the flue gas 16, and the periodic sweeping swing of the fluid self-oscillation device is t 1 / 4T At this moment, the oscillating flow main stream 23 is in the middle of the outflow expansion section 10 and interacts with the flue gas 16 to form a new t 1 / 4T The secondary vortex 24 is generated by the oscillating flow and the smoke at time t = 0T. 0T The secondary vortex 15 generated by the action of the oscillating flow and the smoke is transformed into t 0T The moment oscillating flow and smoke act on the tail vortex 25 and approach the downstream;

[0071] At time t=1 / 2T, the powdered desulfurization catalyst 1 and the feedback flow 18 generate t in the fluid mixing chamber 8. 1 / 2T At the moment, the fluid mixing chamber vortex 27, the periodic sweeping oscillation formed by the fluid self-oscillation device 1 / 2T The oscillating flow main stream 28 at time t is close to the downstream direction of the flue gas. 1 / 4TThe oscillating flow and the smoke react to the secondary vortex 24 at this time, and the t 1 / 2T The secondary vortex 29 generated by the feedback flow and the smoke is close to the upstream side of the smoke flow direction, and a t is formed in the fluid feedback channel 4 close to the upstream side of the smoke 16 flow direction. 1 / 2T The feedback flow 18 dominated by the main feedback flow 26 at the moment flows back to the fluid inlet section 3;

[0072] At time t=3 / 4T, the t 1 / 2T At time t, the main flow 26 of the feedback flow returns from the fluid feedback channel 4 to the fluid inlet section 3 to form 3 / 4T The main stream 30 is fed back at all times and merges with the powdered desulfurization catalyst 1 at the fluid inlet section 3, so that the powdered desulfurization catalyst 1 and t 3 / 4T The main flow 30 is fed back to the fluid mixing chamber 8 to generate a new t 3 / 4T Feedback of the mainstream and the secondary vortex 31 and t of the powdered desulfurization catalyst 3 / 4T At time t 3 / 4T The secondary vortex 31 of the main flow and the powdered desulfurization catalyst is close to the upstream side of the flue gas 16 flow direction, and the periodic sweeping swing formed by the self-oscillation device of the fluid is t 3 / 4T At this moment, the oscillating flow main stream 33 is in the middle of the outflow gradually expanding section 10 and interacts with the smoke to form a new t 3 / 4T The secondary vortex 34 is generated by the oscillating flow and the smoke at time t = 1 / 2T. 1 / 2T The secondary vortex 29 generated by the momentary feedback flow and smoke is transformed into t 1 / 2T The moment oscillating flow and smoke act on the tail vortex 35 and approach the downstream;

[0073] Then it returns to the state at time t=0T, completing a periodic oscillation of a period T.

[0074] Specifically, the SO2 concentration is 200mg / Nm 3 The flue gas, with a flue gas temperature of 150°C, is passed into the desulfurization reactor and mixed with the desulfurizer powder sprayed from the pipeline. After the desulfurization reaction, the desulfurized flue gas 17 is formed and enters the bag dust collector to obtain clean flue gas, which is then transported to the chimney through the fan and discharged into the atmosphere.

[0075] In order to improve the utilization rate of the desulfurizer, the present embodiment provides a method for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation. A fluid self-oscillation device is installed at the desulfurizer injection port. The periodic oscillating and swinging fluid formed by the fluid self-oscillation device can significantly increase the interaction between the powdered desulfurization catalyst and the flue gas, improve the mixed contact between the powdered desulfurizer and SO2 in the flue gas, increase the residence time of the desulfurizer, and improve the reaction degree between the desulfurizer and SO2; the periodic oscillating and swinging fluid formed by the fluid self-oscillation device can break up the agglomerated desulfurizer, and improve the mixed contact between SO2 in the flue gas and the internal powdered desulfurization catalyst; at the same time, the powdered desulfurization catalyst can separate the CaSO4 solid generated by the reaction of the powdered desulfurization catalyst and SO2 and covering the surface of the desulfurizer by oscillation through the periodic oscillating and swinging fluid formed by the fluid self-oscillation device, thereby improving the exposure of the unreacted desulfurizer inside and improving the mixed contact between the desulfurizer and SO2 in the flue gas, thereby achieving the purpose of improving the efficiency of calcium-based dry desulfurization.

[0076] like Fig.11 and Fig.12 As shown, in this embodiment, when the flue gas volume is 30000Nm 3 / h, when the internal pressure of the desulfurization reactor is -6000Pa and the inlet pressure of the fluid oscillator is 10000Pa, it can be verified through CFD simulation that the fluid self-oscillation device sprays the high-viscosity powdered desulfurization catalyst into the desulfurization reactor to form a periodic sweeping oscillating fluid with a certain sweep angle (φ), and reacts with the flue gas to form a secondary vortex, so as to increase the residence time of the desulfurizer from less than 1s to more than 4s, thereby improving the reaction efficiency of the desulfurizer and SO2, breaking up the agglomerated desulfurizer, exposing the unreacted desulfurizer inside, and increasing the calcium-based dry desulfurization efficiency from 70% to 95%; and significantly improving the utilization efficiency of the desulfurizer, which can increase the SO2 concentration in the flue gas from 400mg / Nm 3 Reduced to 20mg / Nm 3 , meeting the national requirements for ultra-low emissions of flue gas SO2 (<35mg / Nm 3 ) requirements.

[0077] Example 2

[0078] See also Figure 7 This embodiment further discloses a specific application scenario of the fluid self-oscillation device. The SO2 concentration in the flue gas is 250 mg / Nm 3 The flue gas temperature is 120°C, and is passed into the desulfurization reactor 51, and mixed with the desulfurizer powder sprayed from the powdered desulfurization catalyst delivery pipeline 50. After the desulfurization reaction, the desulfurized flue gas 17 is formed and enters the bag filter to obtain clean flue gas, which is then transported to the chimney through the fan and discharged into the atmosphere.

[0079] In order to improve the utilization rate of the desulfurization agent, a fluid self-oscillation device 9 is installed at the injection port of the powdered desulfurization catalyst delivery pipeline 50, the powdered desulfurization catalyst delivery pipeline 50 is connected to the inlet of the shell, and the outlet of the shell (i.e., the outflow expansion section 10) is connected to the desulfurization reactor 51 as an injection port of the powdered desulfurization catalyst;

[0080] The shell inlet dimension H1 (36) is 100 mm, the fluid inlet section dimension H2 (37) is 150 mm, the fluid outlet section dimension H5 (40) is 120 mm, the fluid outlet expansion section large diameter end dimension H6 (41) is 600 mm, and the fluid outlet expansion section opening angle β44 is 150°.

[0081] The circumferential dimension H3 (maximum inner diameter of the fluid mixing chamber) 38 of the fluid mixing chamber is 500 mm, the length dimension L3 (45) of the fluid mixing chamber is 500 mm, the mixing chamber expansion angle α46 of the hole section connecting the fluid mixing chamber to the fluid inlet section is 120°, the fluid feedback channel dimension H7 (47) is 150 mm, and the fluid feedback channel outlet dimension L1 (42) is 120 mm;

[0082] The shell length dimension L2 (43) is 840 mm, and the shell circumferential dimension H4 (39) is 800 mm.

[0083] The highly viscous powdered desulfurization catalyst 1 forms a periodic sweeping swing under the action of the fluid self-oscillation device 49, which breaks up the agglomerated desulfurizer, improves the mixed contact between SO2 in the flue gas and the internal desulfurizer, and increases the exposure of the internal unreacted desulfurizer, thereby achieving the purpose of improving the efficiency of calcium-based dry desulfurization.

[0084] Example 3

[0085] See also Figure 8-Figure 9 In this embodiment, based on the first embodiment, a plurality of active ejectors spaced apart along the circumferential direction are provided on the inner wall of the fluid mixing chamber 8, so as to utilize the active ejectors to control the periodic oscillation of the fluid, thereby adapting to the fluctuation of SO2 concentration in the flue gas.

[0086] A CEMS system (flue gas automatic monitoring system) for monitoring flue gas parameters is provided at the flue gas inlet and flue gas outlet of the desulfurization reactor, and / or the chimney outlet, and the CEMS system and the active injector are connected to the control system so as to control the active injector in coordination with the control system according to the monitoring status of the CEMS system.

[0087] Specifically, when the flue gas temperature is 110°C, the SO2 concentration in the flue gas at the desulfurization reactor inlet suddenly increases from 200 mg / Nm 3 Increase to 300mg / Nm 3, which causes the SO2 concentration in the chimney outlet flue gas to suddenly drop from 10mg / Nm 3 Increase to 50mg / Nm 3 The CEMS system immediately detects that the SO2 in the flue gas at the chimney outlet exceeds the standard and feeds back the signal to the control system; in order to meet the ultra-low emission requirements even when the SO2 concentration in the flue gas fluctuates, the control system immediately controls the active injector 6 to inject a flow rate of 1500Nm into the fluid self-oscillation device. 3 / h of jet flue gas, the oscillation period T of the periodic oscillating fluid formed by the fluid self-oscillation device is reduced from 0.12s to 0.1s, and the frequency v is increased from 50Hz to 60Hz, so as to achieve the purpose of improving the efficiency of the desulfurization reaction and adapting to the fluctuation of SO2 concentration in the flue gas.

[0088] Example 4

[0089] See also Figure 8 to Figure 10 In this embodiment, based on the embodiment 3, a plurality of flow spoilers 7 arranged at intervals in the circumferential direction are provided on the inner wall of the fluid mixing chamber 8, and then the active ejector 6 and the fluid spoiler 7 cooperate with the fluid self-oscillation device 49 to achieve the purpose of achieving the same desulfurization efficiency under the supply of desulfurizer at a smaller dosage.

[0090] Specifically, the SO2 concentration in the flue gas is 250mg / Nm 3 The flue gas temperature is 140℃, and it is passed into the desulfurization reactor and mixed with the desulfurizer powder sprayed from the pipeline. After the desulfurization reaction, it enters the bag filter to obtain clean flue gas, which is then transported to the chimney through the fan and discharged into the atmosphere.

[0091] Specifically, in order to improve the utilization rate of the desulfurizer, six active injectors 6 are arranged along the circumferential direction on the inner wall of the fluid mixing chamber 8, the distance between the installation position of the active injector and the fluid inlet section 3 is 30 mm, and the angle between the active injector 6 and the inner wall of the installation position is 10°;

[0092] At the same time, six pairs of fluid spoilers 7 are arranged along the circumferential direction on the inner wall of the fluid mixing chamber 8, two fluid spoilers 7 form a pair, the installation position of the flow spoiler 7 is 100 mm away from the fluid inlet section 3, and the angle between the flow spoiler 7 and the inner wall of the installation position is 5°, so as to improve the fluid mixing effect of the fluid mixing chamber.

[0093] like Fig. 9As shown, the active injector 6 has an active injector front end inlet 62 connected to an external jet gas pipeline and an active injector tail injection port 64 for injecting jet gas, and an active injector inclined surface 63 is provided on the side of the active injector 6 away from the inner wall of the fluid mixing chamber 8 to avoid interfering with the operation of the powdered desulfurization catalyst 1, and an active injector injection tail flow 61 is formed by injecting the jet gas.

[0094] Furthermore, the tail injection port 62 of the active injector shown is a multi-fluid nozzle, and the diameter of the spray droplets of the multi-fluid nozzle is not greater than 50 microns.

[0095] like Fig.10 As shown, the flow spoiler 7 is a convex structure with sloped surfaces at both ends and a circular arc surface (flow spoiler top structure 73) in the middle, and the length of the slope surface of the flow spoiler tail structure 74 near the outlet section of the fluid mixing chamber 8 is greater than the length of the slope surface at the other end. The inclination angle 72 of the flow spoiler is 85°, and the flow spoiler top structure 73 is a circular arc surface or a pointed angle or other similar structures that can produce obvious flow disturbance in the flow field, and the height of the fluid spoiler is 4mm. The tail structure 74 of the flow spoiler is a sloped surface, and the arrangement spacing of adjacent flow spoilers is 5mm, and the arrangement angle 75 of adjacent spoilers is 30°, and then the flow spoiler disturbs the tail flow 71 at the tail of the flow spoiler 7 to enhance the fluid mixing effect of the fluid mixing chamber.

[0096] During operation, the active injector 6 injects a flow rate of 1800 Nm into the fluid self-oscillating device. 3 / h of nitrogen jet gas, the period T of the periodic sweeping oscillating flow formed by the fluid self-oscillation device is reduced from 0.25s to 0.12s, and the frequency v is increased from 25Hz to 50Hz, so that the periodic sweeping oscillating fluid curve at the outlet of the control fluid self-oscillation device is shown as the oscillation flow periodic oscillation curve 49, achieving the purpose of achieving the same desulfurization efficiency as the original straight pipe injection of a large amount of desulfurizer under the condition that the desulfurizer supply is reduced by 10%.

[0097] Example 5

[0098] See also Fig.13 The difference between this embodiment and embodiment 1 is that in this embodiment, the flow dividing island 5 arranged in the inner cavity of the housing 1 is replaced by a naked fluid mixing housing 500, and the fluid mixing housing 500 and the fluid feedback channel 4 are replaced by two fluid feedback pipes 510 arranged outside the fluid mixing housing 500 and connected to both ends of the fluid mixing housing 500, and the two fluid feedback pipes 510 are arranged in parallel, preferably arranged oppositely, so as to form the main flow of feedback flow in opposite directions;

[0099] The fluid mixing shell 500 is a hollow shell with two ends connected to form a fluid mixing chamber 8 in the inner cavity of the fluid mixing shell 500. One end of the fluid mixing shell 500 is an inlet connected to the powdered desulfurization catalyst delivery pipeline 50, and the other end is an outlet connected to the desulfurization reactor 51. A fluid inlet section 3 is provided at the inlet of the fluid mixing shell 500, and a fluid outlet section 9 and an outflow expansion section 10 arranged along the flow direction of the powdered desulfurization catalyst are provided at the outlet. One end of the fluid feedback pipeline 510 is connected to the side of the inlet of the fluid mixing shell 500 close to the powdered desulfurization catalyst delivery pipeline 50, so that the feedback flow enters the fluid mixing chamber 8 through the fluid inlet section 3, and the other end is connected to the outlet of the fluid mixing shell 500 close to the fluid outlet section 9, so that part of the vortex fluid in the fluid mixing chamber 8 forms a feedback flow 18 through the fluid feedback pipeline 510 under the flow limiting effect of the fluid outlet section 9 and flows back to the fluid inlet section 3.

[0100] Example 6

[0101] See also Fig.14 The difference between this embodiment and embodiment 5 is that the two fluid feedback pipes 510 are replaced by a fluid feedback combination pipe 511 composed of a plurality of fluid feedback pipes 510 evenly arranged along the circumferential direction of the fluid mixing shell 500, and the plurality of fluid feedback pipes 510 in the fluid feedback combination pipe 511 are arranged relative to each other.

[0102] Finally, it should be noted that the above embodiments are only used to illustrate the technical solution of the present invention rather than to limit it. Although the present invention has been described in detail with reference to the preferred embodiments, those skilled in the art should understand that the technical solution of the present invention can be modified or replaced by equivalents without departing from the purpose and scope of the technical solution, which should be included in the scope of the claims of the present invention.

Claims

1. A device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation, comprising a powdered desulfurization catalyst delivery pipeline and a desulfurization reactor, characterized in that: It also includes a fluid self-oscillation device connected between the powdered desulfurization catalyst delivery pipeline and the desulfurization reactor; The fluid self-oscillation device comprises a fluid mixing chamber and a fluid feedback channel, the two ends of the fluid mixing chamber are respectively connected to the powdered desulfurization catalyst delivery pipeline and the desulfurization reactor, and a fluid inlet section is provided at one end of the fluid mixing chamber close to the powdered desulfurization catalyst delivery pipeline, and a fluid outlet section and an outflow gradually expanding section are sequentially provided at one end of the fluid mixing chamber close to the desulfurization reactor, and the large end of the outflow gradually expanding section is connected to the desulfurization reactor; One end of the fluid feedback channel is connected to the fluid inlet section on the fluid mixing chamber, and the other end of the fluid feedback channel is connected to the fluid outlet section on the fluid mixing chamber to form a feedback flow in the fluid mixing chamber from the fluid outlet section to the powdered desulfurization catalyst delivery pipeline and the fluid inlet section.

2. The device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 1 is characterized in that: The fluid self-oscillation device comprises a shell and a flow-dividing island which is suspended in an annular manner in the inner cavity of the shell. The flow-dividing island and the shell are both hollow shells with two ends connected, so as to form a fluid mixing chamber in the inner cavity of the flow-dividing island, and an annular channel connecting the two ends of the fluid mixing chamber is formed between the flow-dividing island and the shell to serve as a fluid feedback channel; The shell has an inlet connected to the powdered desulfurization catalyst delivery pipeline and an outlet connected to the desulfurization reactor, and a fluid outlet section and an outflow expansion section are provided at the outlet of the shell, and the end of the diverter island close to the shell inlet is set as the fluid inlet section, and the inlet, fluid inlet section, fluid outlet section and outflow expansion section of the shell are coaxially arranged.

3. The device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 2 is characterized in that: The size H1 of the shell inlet is 50-2000 mm, and the relationship between the size H2 of the fluid inlet section and H1 is H1:H2=1:1-2; The relationship between the circumferential dimension H3 of the fluid mixing chamber and H1 is H1:H3=1:2-6, the relationship between the length dimension L3 of the fluid mixing chamber and H1 is H1:L3=1:1.5-6, and the mixing chamber expansion angle α of the hole section connecting the fluid mixing chamber to the fluid inlet section is 110-170°; The relationship between the shell length dimension L2 and H1 is H1:L2=1:6~12, and the relationship between the shell circumferential dimension H4 and H1 is H1:H4=1:5~15; The relationship between the fluid outlet section dimensions H5 and H1 is H1:H5=1:1~2, the relationship between the fluid outlet gradually expanding section large diameter end dimensions H6 and H1 is H1:H6=1:6~10, and the fluid outlet gradually expanding section opening angle β is 90~170°; The relationship between the fluid feedback channel size H7 and H1 is H1:H7=1:1~2.5, and the relationship between the fluid feedback channel outlet size L1 and H1 is H1:L1=1:1~1.

5.

4. The device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 3 is characterized in that: A plurality of active injectors are arranged evenly spaced along a circumferential direction on the inner wall of the fluid mixing chamber to inject jet gas into the fluid mixing chamber.

5. The device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 4 is characterized in that: The active ejector is connected to a fluid supply facility that provides jet gas to the active ejector, and the fluid supply facility is connected to a control system. The control system is also connected to a CEMS system that is respectively arranged at the flue gas inlet and the flue gas outlet of the desulfurization reactor, so that the control system can dynamically adjust the fluid supply facility according to the monitoring data of the CEMS system, and then dynamically adjust the jet gas of the active ejector.

6. The device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 4, characterized in that: The distance between the active ejector and the fluid inlet section is D1, and D1:L3=0.2-0.3, and the angle between the central axis of the active ejector and the corresponding wall profile at its installation position on the inner wall of the fluid mixing chamber is -10-10°.

7. The device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 4, characterized in that: The injection head of the active injector is a multi-fluid nozzle, and the diameter of the droplets sprayed by the multi-fluid nozzle is not greater than 50 microns.

8. The device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 3, characterized in that: A plurality of flow spoilers are arranged at intervals along the circumferential direction and the wall profile direction on the inner wall of the fluid mixing chamber to form a turbulent flow in the fluid mixing chamber.

9. The device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 8, characterized in that: The distance between the flow spoiler and the fluid inlet section is D2, and D2:L3=0.45-0.8, and the angle between the central axis of the flow spoiler and the corresponding wall profile at the installation position on the inner wall of the fluid mixing chamber is -4-12°.

10. The device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 1, characterized in that: The fluid self-oscillation device comprises a fluid mixing housing and at least two fluid feedback pipes arranged in parallel outside the fluid mixing housing; The fluid mixing shell is a hollow shell with two ends connected to form a fluid mixing chamber in the inner cavity of the fluid mixing shell. One end of the fluid mixing shell is an inlet connected to the powdered desulfurization catalyst delivery pipeline, and the other end is an outlet connected to the desulfurization reactor. A fluid inlet section is provided at the inlet of the fluid mixing shell, and a fluid outlet section and an outflow expansion section arranged along the flow direction of the powdered desulfurization catalyst are provided at the outlet. One end of the fluid feedback pipeline is connected to the side of the inlet of the fluid mixing shell close to the powdered desulfurization catalyst delivery pipeline, and the other end is connected to the outlet of the fluid mixing shell close to the fluid outlet section.

11. A method for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation, characterized in that: The device for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to any one of claims 1 to 10 specifically comprises the following steps: Step 1. The powdered desulfurization catalyst in the powdered desulfurization catalyst delivery pipeline is sprayed into the fluid self-oscillation device under the action of a fan, and then sprayed into the desulfurization reactor after forming a periodic sweeping and swinging fluid in the outflow expansion section of the fluid self-oscillation device to form a desulfurization reaction zone, and a secondary vortex is formed by the periodic sweeping and swinging fluid and the flue gas in the desulfurization reactor to increase the mixing contact and residence time of the powdered desulfurizer and the flue gas.

12. The method for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 11, characterized in that: Also includes step 2, Step 2: After the powdered desulfurization catalyst reacts with the flue gas in the desulfurization reactor, the desulfurized flue gas is transported to a dust collector for dust removal to obtain clean flue gas, and then the clean flue gas is discharged into the atmosphere through a chimney.

13. The method for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 11, characterized in that: The period of the periodic sweeping and oscillating fluid is T; At time t=0T, the mainstream direction of the periodically sweeping and oscillating fluid is close to the upstream of the smoke, and interacts with the smoke to form a secondary vortex close to the downstream of the smoke; At time t=1 / 4T, the mainstream direction of the periodically swept oscillating fluid is in the middle of the outflow expansion section, and reacts with the smoke to form a new secondary vortex close to the upstream of the smoke, while the tail vortex formed by the secondary vortex at time t=0T is close to the downstream of the smoke; At time t=1 / 2T, the mainstream direction of the periodically sweeping and oscillating fluid is close to the downstream of the smoke, and interacts with the smoke to form a secondary vortex close to the upstream of the smoke; At time t=3 / 4T, the mainstream direction of the periodically swept oscillating fluid is in the middle of the outflow expansion section, and interacts with the smoke to form a new secondary vortex close to the upstream of the smoke. At the same time, the tail vortex formed by the secondary vortex at t=1 / 2T is close to the downstream of the smoke.

14. The method for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 11, characterized in that: Spraying jet gas into the fluid mixing chamber through a plurality of active ejectors evenly spaced along the circumferential direction on the inner wall of the fluid mixing chamber; The active ejector is connected to a fluid supply facility that provides jet gas to the active ejector, and the fluid supply facility is connected to a control system. The control system is also connected to a CEMS system that is respectively arranged at the flue gas inlet and the chimney outlet in the desulfurization reactor, so that the control system can dynamically adjust the fluid supply facility according to the monitoring data of the CEMS system, and then dynamically adjust the jet gas of the active ejector, and then actively regulate the period T, frequency v and sweeping angle of the periodic sweeping oscillating fluid formed by the fluid self-oscillation device.

15. The method for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 14, characterized in that: The jet gas is air or flue gas or nitrogen.

16. The method for improving the efficiency of calcium-based dry desulfurization by utilizing fluid self-oscillation according to claim 12, characterized in that: The temperature of the desulfurization reaction zone is controlled between 50°C and 350°C, the powdered desulfurization catalyst is a calcium-based desulfurizer, and the flue gas has a SO2 concentration of less than 400 mg / Nm 3 of smoke.

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