Flue gas desulfurization, denitrification, dust removal and separation equipment

Abstract

The invention relates to the technical field of flue gas purification, in particular to flue gas desulfurization, denitrification and dust removal separation equipment which comprises a separation mechanism, a laminar flow reactor, a mixed flow impeller and a desulfurization reactor. The separation mechanism is connected with the air inlet pipeline; the laminar flow reactor is connected with the separation mechanism; the mixed flow impeller is connected between the separation mechanism and the laminar flow reactor; the desulfurization reactor is connected with the laminar flow reactor; oily particles are preliminarily separated through centrifugal force, after flue gas internally rotates and ascends, a secondary filter screen is driven by the ascending force of the flue gas to shake at high frequency to secondarily filter the oily particles, meanwhile, the oily particles are separated again through the internal rotation force of the flue gas, and the flue gas and ammonia gas are fully mixed and pre-distributed through a mixed flow impeller, so that the denitration efficiency is improved; the problems that the catalyst is damaged due to the fact that oily particles in flue gas cannot be effectively filtered, and the denitration efficiency is reduced due to non-uniform distribution when the flue gas reaches a fluidized bed are solved.

Description

Technical Field

[0001] The invention relates to the technical field of flue gas purification, and in particular to a flue gas desulfurization, denitrification, dust removal and separation device. Background Art

[0002] Flue gas desulfurization, denitrification and dust removal separation equipment is an industrial production environmental protection equipment integrating desulfurization, denitrification and dust removal functions. It is mainly used to remove harmful substances such as sulfur oxides, nitrogen oxides and particulate matter in flue gas. It is widely used in flue gas treatment in the fields of electricity, steel, chemical industry, etc., and is of great significance to reducing air pollution and protecting the environment.

[0003] At present, industrial desulfurization, denitrification and dust removal are usually carried out in steps. The desulfurization process is usually divided into two methods: wet desulfurization and dry desulfurization. Compared with the dry desulfurization method of converting sulfur dioxide into sulfuric acid by activated carbon adsorption or catalyst, the wet desulfurization using limestone slurry has higher desulfurization efficiency, but the cost is also higher and the area occupied is large. In the denitrification process, the selective catalytic reduction denitrification (SCR) technology is commonly used. Ammonia is injected into the flue gas to react with nitrogen oxides to generate nitrogen and water. The desulfurization efficiency of this method is high. High and wide range of applications; in the dust removal process, common dust removal methods include gravity sedimentation, bag dust removal and electrostatic precipitator. The dust removal efficiency of electrostatic precipitator can reach 99%, but the electrostatic precipitator equipment is large and occupies a large area. The bag dust removal equipment is compact and flexible in operation. However, compared with electrostatic precipitator, its operation and maintenance costs are high, energy consumption is high and the filter bag life is short. The investment cost is about 1.5 to 2 times that of electrostatic precipitator. Combining the above steps, it can be seen that the current desulfurization, denitrification and dust removal steps will generate a large floor space and increase the maintenance cost. The technology of nitrate removal has begun to develop in the direction of integration. In order to save space, the integrated desulfurization, denitrification and dust removal device usually uses a circulating fluidized bed (CFB) for desulfurization and denitrification reactions. The fluidized bed is a bed formed by stacking solid particles on a porous distribution plate, so that the fluid passes through the bed from bottom to top. In the process of denitrification, after the flue gas passes through the catalyst of the fluidized bed, the solid particles are blown up by the flue gas and suspended, increasing the surface area of ​​the catalyst in contact with the flue gas, so as to achieve full reaction and denitrification. However, in this process, since the flue gas carries particulate matter, the fluidization effect of the bed will decrease, and the particulate matter will cover the surface of the catalyst and affect the catalytic activity, thereby reducing the denitrification efficiency. The prior art has proposed a good solution, such as a desulfurization, denitrification and dust removal integrated laminar flow reactor with patent publication number CN114589007B, which is provided with a filter screen to filter the particulate matter inside the flue gas before it enters the fluidized bed, and the particulate matter on the filter screen is scraped out by a scraper to avoid clogging, thereby reducing the impact of solid particulate matter in the flue gas on the fluidized bed.

[0004] Although the existing technology solves the problem that solid particles in the flue gas enter the laminar flow reactor and cause mechanical wear between the catalysts in the fluidized bed, reducing the life of the catalyst and thus causing a decrease in the denitrification efficiency, the following problems still exist: the coke oven flue gas will carry oily components (such as tar). Although the scraper can scrape off the particles attached to the filter, the oily substance cannot be removed well. At this time, on the one hand, the filter will be blocked, affecting the air intake efficiency, resulting in uneven distribution of the flue gas when it reaches the fluidized bed, thereby causing a decrease in the denitrification efficiency; on the other hand, after the oily particles come into contact with the denitrification catalyst with the flue gas, due to the large number of micropores on the surface of the denitrification catalyst, the oily particles will cause physical blockage on the catalyst surface due to their viscosity and adhesion, and at the same time cover the active sites on the catalyst surface. In addition, since the flue gas needs to be kept between 300 and 420 degrees Celsius during the denitrification process, the oily particles will cause catalyst sintering at high temperatures, thereby making the catalyst unable to effectively participate in the catalytic reaction, resulting in a decrease in the denitrification efficiency.

[0005] In view of the above situation, in order to overcome the above technical problems, the present invention provides a flue gas desulfurization, denitrification, dust removal and separation equipment. Summary of the invention

[0006] The present invention provides a flue gas desulfurization, denitrification, dust removal and separation equipment, which solves the problem that oily particles in the flue gas cannot be effectively filtered, resulting in damage to the catalyst and the flue gas is unevenly distributed when it reaches the fluidized bed, thereby reducing the denitrification efficiency. The oily particles are initially separated by centrifugal force, and when the flue gas rises inwardly, the rising force of the flue gas drives the secondary filter screen to vibrate at a high frequency to perform a secondary filtration, while the internal rotation force of the flue gas is used to separate the oily particles again, and the flue gas and ammonia are fully mixed and pre-distributed through a mixed flow impeller, thereby improving the denitrification efficiency.

[0007] In order to achieve the above object, the present invention provides the following technical solutions:

[0008] A flue gas desulfurization, denitrification and dust removal separation device, comprising an air intake pipe, an ammonia channel and an air outlet channel; further comprising a separation mechanism, a laminar flow reactor, a mixed flow impeller and a desulfurization reactor; the separation mechanism is connected to the air intake pipe; the laminar flow reactor is connected to the separation mechanism; the mixed flow impeller is connected between the separation mechanism and the laminar flow reactor; the desulfurization reactor is connected to the laminar flow reactor; the flue gas enters the separation mechanism through the air intake pipe and performs downward swirling flow to separate solid particles and oily particles from the flue gas by centrifugal force, and when the flue gas reaches the bottom of the separation mechanism, the inner circle Negative pressure is formed, which causes the ammonia to swirl inward and rise; ammonia enters the laminar flow reactor from the ammonia channel and swirls downward. When the ammonia reaches the bottom of the laminar flow reactor, negative pressure is formed in the inner circle, which causes the ammonia to swirl inward and rise in the opposite direction to the rotation of the flue gas. The inward rotation and rise of ammonia drives the mixed flow impeller to rotate. The rotation of the mixed flow impeller causes the ammonia and flue gas to be fully mixed and enter the upper layer of the laminar flow reactor with an upward trend. The rising force of the ammonia and flue gas drives the separation mechanism to vibrate, separate the fine particles carried by the flue gas during the rising process, and filter out the catalyst carried by the flue gas that has completed denitrification.

[0009] Preferably, the separation mechanism includes a shell, an ascending channel, a dust storage chamber and an adsorption plate; the shell is connected to the air intake duct, the shell has a cylindrical structure at the upper part, an inverted cone structure at the lower part, and the air intake duct is tangentially connected to the upper cylindrical structure; the ascending channel is arranged at the central position inside the shell; the dust storage chamber is connected to the lower part of the shell; the adsorption plate is rotatably mounted on the inner wall of the shell.

[0010] In the above scheme, the flue gas enters the shell from the air intake duct along a trajectory tangent to the upper cylindrical structure of the shell, and forms a spiral downward flow direction through the inverted cone structure at the bottom of the shell. During the flow, the internal particles are thrown onto the inner wall by centrifugal force and fall along the inner wall to the dust storage chamber under the action of the airflow, thereby separating the solid particles and oily particles in the flue gas. When the flue gas reaches the bottom of the inverted cone structure, the outward-circling flue gas rotates under the restriction of the inner wall of the inverted cone structure and the action of centrifugal force, and the particles in the flue gas are pushed to the inner wall of the shell, resulting in a decrease in air density in the central area, thereby forming a negative pressure, and forming a negative pressure zone in the center of the cone bottom, so that the flue gas reaching the bottom of the inverted cone structure changes direction under the action of the negative pressure zone and the inner wall of the bottom of the inverted cone structure, forming an inward-circling upward airflow, so that the flue gas that has completed dust removal rises and flows out.

[0011] Preferably, the adsorption plate has adsorption holes on its surface, and has oil-repellent channels and oil-collecting spaces inside; the adsorption holes are inverted cone-shaped structures, and the end with a larger aperture faces the outside of the adsorption plate.

[0012] In the above scheme, the flue gas rotating downward from the outer circle causes the adsorption plate to rotate and capture the oily particles, thereby ensuring that the oily particles can be quickly separated and the oily particles in the flue gas cannot cause damage to the catalyst.

[0013] Preferably, the ascending channel includes a tube body, a filter chute, a secondary filter and an oscillation spring; the tube body is connected to the laminar flow reactor; the filter chute is opened at the lower part of the tube body; the secondary filter is slidably installed in the filter chute, and the secondary filter is a rigid structure; the oscillation spring is connected to the secondary filter.

[0014] In the above scheme, the secondary filter can be used to perform secondary filtration on the fine particles carried in the rising inward swirling airflow, thereby ensuring the dust removal effect and preventing the flue gas entering the denitrification process from causing damage to the catalyst; the secondary filter can be vibrated by the vibration spring to shake off the fine dust attached to the lower surface of the secondary filter, thereby avoiding clogging of the secondary filter after continuous operation.

[0015] Preferably, a sealing ring is provided at the edge of the secondary filter; the oscillation spring includes a vibration spring and a balance spring; the vibration springs are installed in a circular array above the edge of the secondary filter; and the balance springs are installed in a circular array with the same number below the edge of the secondary filter.

[0016] In the above scheme, a sealing ring is provided on the edge of the secondary filter to prevent particles from entering the filter chute and causing particle accumulation at the filter chute position; a vibration spring and a balancing spring circular array are installed on the upper and lower sides of the edge of the secondary filter, so that the secondary filter can maintain a balanced state without shaking when smoke is not passed in, and when the rising smoke contacts the secondary filter, the rising force will destroy the balanced state, and since the flow rate of the rising smoke is changing all the time, the rising force generated is also changing all the time. At this time, the secondary filter continues to vibrate at a high frequency under the change of the rising force, so that the filtered particles cannot adhere to the secondary filter, and since the rising smoke in the inner circle is rotating and rising, the particles that cannot adhere to the secondary filter will be thrown to the outer circle by the centrifugal force, and when they reach the outer rotating sinking smoke position of the outer circle, they will be thrown to the inner wall of the shell by the centrifugal force for sedimentation.

[0017] Preferably, the laminar flow reactor includes an ammonia mixing layer, a catalytic layer and an outflow layer; the ammonia mixing layer includes a mixing chamber and a mixing tube; the lower part of the mixing chamber is connected to the ascending channel, the upper part of the inner wall of the mixing chamber is a cylindrical structure, the lower part is an inverted cone structure, and the ammonia channel is tangentially connected to the mixing chamber; the mixing tube is connected to the upper part of the mixing chamber; the catalytic layer includes an inverted cone section, a fine porous plate and a catalytic bed; the inverted cone section is connected to the ammonia mixing layer; the fine porous plate is connected to the inverted cone section; the catalytic bed is arranged on the upper side of the fine porous plate; the outflow layer is arranged at the upper end of the catalytic layer.

[0018] In the above scheme, ammonia enters the mixing chamber through the ammonia channel in a tangential trajectory to the mixing chamber, so that the outer circle forms a rotating downward movement trend under the guidance of the inner wall of the mixing chamber, and reaches the bottom of the mixing chamber to form an inward rotation and rise. At this time, the flue gas and ammonia rotating and rising in the ascending channel are both in a rotating state and are in the same position, so that they are mixed more fully.

[0019] Preferably, the mixing tube is an inverted cone structure; the axis of the mixed flow impeller coincides with the axis of the rising channel and the mixing tube, the radius of the mixed flow impeller is slightly smaller than the radius of the bottom of the mixing tube and larger than the radius of the rising channel, and the horizontal plane where the upper end surface of the mixed flow impeller is located is higher than the horizontal plane where the lower end of the mixing tube is located.

[0020] In the above scheme, the rising flue gas in the ascending channel and the ammonia forming an inward rotation are mixed by a mixed flow impeller. Since the blades of the mixed flow impeller are of a mixed flow structure, it can combine the advantages of the axial flow fan and the centrifugal fan to achieve the mixing of ammonia and flue gas while entering the catalyst layer with the trend of axial flow diffusion, completing the pre-distribution of the mixed gas of ammonia and flue gas, so that it can fully contact with the catalyst and improve the denitrification efficiency.

[0021] Preferably, the vertical plane where the tangent line between the air intake pipe and the shell is located and the vertical plane where the tangent line between the ammonia passage and the mixing chamber is located are the same vertical plane, and the air intake directions of the two are opposite.

[0022] In the above scheme, the rotation direction formed by the flue gas after entering the air intake duct is opposite to the rotation direction formed by the ammonia after entering the ammonia channel, so that convection is formed after the flue gas and ammonia meet, further improving the mixing effect of the two.

[0023] Preferably, the outflow layer includes a catalyst filter plate and a connecting rod; the catalyst filter plate is arranged on the top of the catalytic layer, and the catalyst filter plate is an elastic metal sheet with pores smaller than the catalyst particle size; the connecting rod is connected between the catalyst filter plate and the secondary filter screen, and passes through the pore plate.

[0024] In the above scheme, by setting up the catalyst filter plate, it can be ensured that the catalyst carried away by the flue gas after completing the denitrification catalytic reaction can be filtered out, and because the catalyst filter plate and the secondary filter are connected, when the secondary filter is vibrating, the catalyst filter plate will also be deformed under the pull of the connecting rod. Since the catalyst filter plate is an elastic metal plate, when it is deformed, it forms a force in a relative direction with the rising force of the flue gas under its own restoring force, thereby causing the catalyst filter plate to vibrate at a high frequency to avoid clogging of the catalyst filter plate.

[0025] Preferably, the secondary filter, catalyst filter plate, connecting rod and mixed flow impeller are made of high temperature resistant lightweight materials; the elastic modulus of the balance spring is sufficient to keep the secondary filter balanced when no flue gas is introduced.

[0026] In the above scheme, the use of high-temperature resistant lightweight materials can ensure that the balance spring can more easily ensure that the secondary filter, catalyst filter plate, connecting rod and mixed flow impeller are in a balanced state when the flue gas is not introduced; because the secondary filter and the catalyst filter plate will be affected by the rising force of the flue gas, and because the secondary filter and the catalyst filter plate are both provided with fine pores on the surface, the contact area between the secondary filter and the catalyst filter plate and the flue gas is large, and the balance state brought by the balance spring can be destroyed under the rising force of the flue gas, so that the secondary filter and the catalyst filter plate can both vibrate at high frequency to keep the lower surface of the secondary filter and the catalyst filter plate from being blocked, and the secondary filter can ensure that the flue gas entering the denitrification step will not damage the catalyst, and at the same time, the catalyst filter plate can filter out the catalyst escaping with the flue gas, thereby reducing the loss of the catalyst and improving the efficiency of denitrification.

[0027] The beneficial effects of the present invention are as follows:

[0028] 1. Compared with the existing flue gas desulfurization, denitration and dust removal separation equipment, the present invention performs a dust removal process before denitration by setting a separation mechanism to prevent ordinary particles and oily particles in the flue gas from damaging the denitration catalyst. The flue gas entering the shell can rotate and sink. During the rotation process, the oily particles and ordinary particles in the flue gas are separated from the inner wall of the shell by centrifugal force. After the flue gas reaches the bottom of the shell, it rotates inward and rises. During the rising process, it is filtered twice. The secondary filter screen maintains balance when the flue gas is not passed in, and the rising force of the rising flue gas will destroy the balance state. At this time, the secondary filter screen is in High-frequency vibration continues to occur under the change of rising force, so that the filtered particles cannot adhere to the secondary filter. Moreover, since the rising flue gas in the inner circle rises in a rotating manner, the particles that cannot adhere to the secondary filter will be thrown to the outer circle by the centrifugal force. When they reach the outward rotating and sinking flue gas position of the outer circle, they will be thrown to the inner wall of the shell by the centrifugal force for sedimentation. On the one hand, it ensures that the filter is always clean and will not be blocked. On the other hand, it can improve the filtering effect of oily particles and ordinary particles in the flue gas, thereby ensuring the normal reaction of the denitrification catalyst, increasing the life of the catalyst, and thus ensuring the denitrification efficiency.

[0029] 2. The present invention sets a mixed flow impeller, which is rotated by the spiral force and rising force of the introduced ammonia. On the one hand, the flue gas that has completed the dust removal process can be guided into the mixing chamber, and the rising negative pressure can be provided to the inward rotation of the flue gas, thereby improving the air intake efficiency of the flue gas. On the other hand, after the ammonia is introduced into the mixing chamber, the outer ring rotates and sinks under the action of the mixing chamber structure, while the inner ring rotates and rises. Moreover, since the ammonia introduction direction is opposite to the flue gas introduction direction, the ammonia and the flue gas rotate in opposite directions to form convection, and are fully mixed under the axial flow guiding action of the mixed flow impeller, thereby improving the denitrification efficiency. Moreover, since the mixed flow impeller can realize both axial flow and centrifugal action, the mixed gas of the flue gas and ammonia can be pre-distributed when it reaches the catalyst layer, thereby making the denitrification reaction more sufficient and improving the denitrification efficiency.

[0030] 3. The present invention filters out the catalyst carried in the flue gas that has completed denitrification by setting a catalyst filter plate to prevent the catalyst from escaping and causing a decrease in the denitrification reaction efficiency. The catalyst filter plate is set as an elastic metal sheet and connected to the secondary filter screen, so that when the secondary filter screen vibrates, it can drive the catalyst filter plate to undergo elastic deformation and shake out the catalyst that blocks the pores of the catalyst filter plate, thereby reducing the loss of the catalyst and improving the denitrification efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] In order to more clearly illustrate the specific implementation methods of the present invention or the technical solutions in the prior art, the drawings required for use in the specific implementation methods or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are some implementation methods of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0032] Figure 1 It is a schematic diagram of the overall structure of the present invention;

[0033] Figure 2 is a sectional view of the separation mechanism structure of the present invention;

[0034] Figure 3 is a cross-sectional view of the internal structure of the adsorption plate of the present invention;

[0035] Figure 4 yes Figure 2 A magnified view of the structure at center;

[0036] Figure 5 is an overall cross-sectional view of the present invention;

[0037] Figure 6 It is the installation position diagram of the mixed flow impeller of the present invention;

[0038] Figure 7 is a smoke flow diagram of the present invention;

[0039] Figure 8 is the ammonia flow diagram of the present invention;

[0040] In the figure: 1. air inlet pipe; 2. ammonia channel; 3. air outlet channel; 4. separation mechanism; 41. shell; 42. rising channel; 421. pipe body; 422. filter chute; 423. secondary filter; 4231. sealing ring; 424. oscillation spring; 4241. vibration spring; 4242. balance spring; 43. dust storage chamber; 44. adsorption plate; 441. adsorption hole; 442. oil-repellent channel; 443. oil-collecting space; 5. laminar flow reactor; 51. ammonia mixing layer; 511. mixing chamber; 512. mixing tube; 52. catalytic layer; 521. inverted cone section; 522. fine-mesh plate; 523. catalytic bed; 53. outflow layer; 531. catalyst filter plate; 532. connecting rod; 6. mixed flow impeller; 7. desulfurization reactor. DETAILED DESCRIPTION

[0041] In order to better understand the above technical solution, the above technical solution will be described in detail below in conjunction with the accompanying drawings and specific implementation methods.

[0042] See also Figures 1 to 8 The present invention provides a flue gas desulfurization, denitrification and dust removal separation equipment, and the technical solution is as follows:

[0043] As a specific embodiment of the present invention, refer to Figure 1 A flue gas desulfurization, denitrification and dust removal separation device, comprising an air intake pipe 1, an ammonia channel 2 and an air outlet channel 3; further comprising a separation mechanism 4, a laminar flow reactor 5, a mixed flow impeller 6 and a desulfurization reactor 7; the separation mechanism 4 is connected to the air intake pipe 1; the laminar flow reactor 5 is connected to the separation mechanism 4; the mixed flow impeller 6 is connected between the separation mechanism 4 and the laminar flow reactor 5; the desulfurization reactor 7 is connected to the laminar flow reactor 5; the flue gas enters the separation mechanism 4 through the air intake pipe 1 and swirls downward to separate solid particles and oily particles from the flue gas by centrifugal force, and when the flue gas reaches the bottom of the separation mechanism 4, a negative pressure is formed in the inner circle, thereby The ammonia enters the laminar flow reactor 5 from the ammonia channel 2 and swirls downward. When the ammonia reaches the bottom of the laminar flow reactor 5, a negative pressure is formed in the inner circle and the ammonia rises inward in a direction opposite to the direction of rotation of the flue gas. The inward rotation and rise of the ammonia drives the mixed flow impeller 6 to rotate. The rotation of the mixed flow impeller 6 makes the ammonia and the flue gas fully mixed and enters the upper layer of the laminar flow reactor 5 with an upward movement trend. The rising force of the ammonia and the flue gas drives the separation mechanism 4 to vibrate and separate the fine particles carried by the flue gas in the rising process again, and filters out the catalyst carried by the flue gas that has completed denitrification. The flue gas that has completed dust removal and denitrification flows to the desulfurization reactor 7 for desulfurization reaction.

[0044] As a specific embodiment of the present invention, refer to Figure 2 and Figure 7 The separation mechanism 4 includes a shell 41, an ascending channel 42, a dust storage chamber 43 and an adsorption plate 44; the shell 41 is connected to the air intake pipe 1, the shell 41 is a cylindrical structure at the upper part, and an inverted cone structure at the lower part, and the air intake pipe 1 is tangentially connected to the upper cylindrical structure; the ascending channel 42 is arranged at the center position inside the shell 41; the dust storage chamber 43 is connected to the lower part of the shell 41; the adsorption plate 44 is rotatably mounted on the inner wall of the shell 41. The flue gas enters the shell 41 from the air intake duct 1 along a trajectory tangent to the upper cylindrical structure of the shell 41, and forms a spiral downward flow direction through the inverted cone structure at the bottom of the shell 41. During the flow, the internal particles are thrown onto the inner wall by centrifugal force and fall along the inner wall to the dust storage chamber 43 under the action of the airflow, thereby separating the solid particles and oily particles in the flue gas. When the flue gas reaches the bottom of the inverted cone structure, the particles in the outward-rotating flue gas are pushed toward the inner wall of the shell 41 due to the restriction of the inner wall of the inverted cone structure and the centrifugal force, resulting in a decrease in the air density in the central area, thereby forming a negative pressure, and forming a negative pressure zone at the center of the cone bottom, so that the flue gas reaching the bottom of the inverted cone structure changes direction under the action of the negative pressure zone and the inner wall of the bottom of the inverted cone structure, forming an inward-rotating upward airflow, so that the flue gas that has completed dust removal rises and flows out, while the solid particles and oily particles will enter the dust storage chamber 43 along the inner wall of the shell 41.

[0045] As a specific embodiment of the present invention, refer to Figure 2 and Figure 3 The adsorption plate 44 has adsorption holes 441 on its surface, and has an oil-repellent channel 442 and an oil-collecting space 443 inside. The adsorption hole 441 is an inverted cone structure, and the end with a larger aperture faces the outside of the adsorption plate 44. The flue gas that descends and rotates through the outer circle causes the adsorption plate 44 to rotate and capture the oily particles, thereby ensuring that the oily particles can be quickly separated and that the oily particles in the flue gas cannot cause damage to the catalyst; and through the inverted cone structure of the adsorption hole 441, the adsorbed oily particles cannot flow out of the adsorption hole 441 after entering the oil collecting space 443, and the oily particles will flow from the oil-repellent channel 442 to the bottom of the shell 41 after gathering in the oil collecting space 443, and flow into the dust storage chamber 43 along the bottom structure. Since the adsorption plate 44 is a freely rotatable structure, the adsorption plate 44 will drive the adsorbed oily particles to gather and maintain a flowing state during the rotation process to avoid blockage. On the other hand, when the adsorption plate 44 rotates, the oily particles attached to the inner wall of the shell 41 will be scraped and gathered, and the adsorption plate 44 itself has an oblique structure, which can make the gathered oily particles flow under the action of the outer circle rotating flue gas and its own gravity, so that they flow into the dust storage chamber 43.

[0046] As a specific embodiment of the present invention, refer to Figure 4 and Figure 7 , the ascending channel 42 includes a tube body 421, a filter chute 422, a secondary filter 423 and an oscillation spring 424; the tube body 421 is connected to the laminar flow reactor 5; the filter chute 422 is provided at the lower part of the tube body 421; the secondary filter 423 is slidably installed in the filter chute 422, and the secondary filter 423 is a rigid structure, and the radius of the filter pores provided on its surface can be changed according to the requirements of particle filtering; the oscillation spring 424 is connected to the secondary filter 423. The secondary filter 423 can be used to perform secondary filtration on the fine particles carried in the ascending inward swirling airflow, thereby ensuring the dust removal effect, so that the flue gas entering the denitrification will not cause damage to the catalyst; the secondary filter 423 can be oscillated by the oscillation spring 424, and the fine dust attached to the lower surface of the secondary filter 423 can be shaken off to avoid clogging of the secondary filter 423 after continuous operation. A sealing ring 4231 is provided at the edge of the secondary filter 423; the vibration spring 424 includes a vibration spring 4241 and a balance spring 4242; the vibration spring 4241 is installed in a circular array above the edge of the secondary filter 423; the balance spring 4242 is installed in a circular array with the same number below the edge of the secondary filter 423. By providing a sealing ring 4231 at the edge of the secondary filter 423, particles are prevented from entering the filter chute 422, causing particle accumulation at the position of the filter chute 422; the vibration spring 4241 and the balance spring 4242 are installed in a circular array on the upper and lower sides of the edge of the secondary filter 423, so that the secondary filter 423 maintains a balanced state without shaking when smoke is not passed in, and when the rising smoke contacts the secondary filter 423, the rising force will destroy the balanced state, and since the flow rate of the rising smoke is constantly changing, the rising force generated is also constantly changing. At this time, the secondary filter 423 continues to vibrate at a high frequency under the change of the rising force, so that the filtered particles cannot adhere to the secondary filter 423, and since the rising smoke of the inner circle is rotating and rising, the particles that cannot adhere to the secondary filter 423 will be thrown to the outer circle by the centrifugal force, and reach the outer rotating sinking smoke position of the outer circle, so that they are thrown to the inner wall of the shell 41 by the centrifugal force again for sedimentation.

[0047] As a specific embodiment of the present invention, refer to Figure 5 , Figure 6 and Figure 8The laminar flow reactor 5 includes an ammonia mixing layer 51, a catalytic layer 52 and an outflow layer 53; the ammonia mixing layer 51 includes a mixing chamber 511 and a mixing tube 512; the lower part of the mixing chamber 511 is connected to the ascending channel 42, the upper part of the inner wall of the mixing chamber 511 is a cylindrical structure, the lower part is an inverted cone structure, and the ammonia channel 2 is tangentially connected to the mixing chamber 511; the mixing tube 512 is connected to the upper part of the mixing chamber 511; the catalytic layer 52 includes an inverted cone section 521, a fine porous plate 522 and a catalytic bed 523; the inverted cone section 521 is connected to the ammonia mixing layer 51; the fine porous plate 522 is connected to the inverted cone section 521; the catalytic bed 523 is arranged on the upper side of the fine porous plate 522; the outflow layer 53 is arranged at the upper end of the catalytic layer 52. Ammonia enters the mixing chamber 511 through the ammonia channel 2 along a tangential trajectory to the mixing chamber 511, so that the outer circle forms a rotating downward movement trend under the guidance of the inner wall of the mixing chamber 511, and reaches the bottom of the mixing chamber 511 to form an inward rotation and rise. At this time, the flue gas and ammonia rotating upward in the rising channel 42 are both in a rotating state and are in the same position, so that they are mixed more fully. The mixing tube 512 is an inverted cone structure; the axis of the mixed flow impeller 6 coincides with the axis of the rising channel 42 and the mixing tube 512, so that the rising path of the flue gas and the inward rotation path of the ammonia are on the same axis, making the mixing more complete. The radius R1 of the mixed flow impeller 6 is slightly smaller than the bottom radius R2 of the mixing tube 512, and larger than the radius R3 of the rising channel 42. The horizontal plane where the upper end surface of the mixed flow impeller 6 is located is higher than the horizontal plane where the lowest end of the mixing tube 512 is located. After the ammonia rises inwardly, its rising force and spiral force drive the mixed flow impeller 6 to rotate, and the ammonia is pumped, so the ammonia flow rate is greater than the flue gas. The mixed flow impeller 6 will rotate in the same direction as the ammonia and mix the rising flue gas and ammonia. At the same time, since the radius of the rising channel 42 is smaller than the radius of the mixed flow impeller 6, the influence of the flue gas on the rotation of the mixed flow impeller 6 will be further reduced at this time. The flue gas rising in the ascending channel 42 and the ammonia forming an inward rotation are mixed by the mixed flow impeller 6. Since the blades of the mixed flow impeller 6 are of a mixed flow structure, it can combine the advantages of the axial flow fan and the centrifugal fan, and cooperate with the inverted cone structure of the mixing tube 512 to achieve the mixing of ammonia and flue gas while entering the catalyst layer 52 with the trend of axial flow diffusion, completing the pre-distribution of the mixed gas of ammonia and flue gas, so that it can fully contact with the catalyst and improve the denitrification efficiency.

[0048] As a specific embodiment of the present invention, refer to Figure 1 , Figure 5 and Figure 8The vertical plane where the tangent line between the air intake pipe 1 and the housing 41 and the vertical plane where the tangent line between the ammonia channel 2 and the mixing chamber 511 are located are the same vertical plane, and the air intake directions of the two are opposite. The rotation direction formed by the flue gas after entering the air intake pipe 1 is opposite to the rotation direction formed by the ammonia after entering the ammonia channel 2, so that convection is formed after the flue gas and ammonia meet, further improving the mixing effect of the two.

[0049] As a specific embodiment of the present invention, refer to Figure 5 , the outflow layer 53 includes a catalyst filter plate 531 and a connecting rod 532; the catalyst filter plate 531 is arranged on the top of the catalytic layer 52, and the catalyst filter plate 531 is an elastic metal sheet with pores smaller than the catalyst particle size, and will not undergo plastic deformation below 450 degrees Celsius; the connecting rod 532 is connected between the catalyst filter plate 531 and the secondary filter screen 423, and penetrates the pore plate 522. By setting the catalyst filter plate 531, it can be ensured that the catalyst carried away by the flue gas after the denitration catalytic reaction is completed can be filtered down, and because the catalyst filter plate 531 and the secondary filter screen 423 are connected, when the secondary filter screen 423 vibrates, the catalyst filter plate 531 will also be deformed under the pull of the connecting rod 532. Since the catalyst filter plate 531 is an elastic metal plate, when it is deformed, it forms a force in a relative direction with the rising force of the flue gas under its own restoring force, so that the catalyst filter plate 531 is shaken at a high frequency to avoid clogging of the catalyst filter plate 531.

[0050] As a specific embodiment of the present invention, refer to Figure 4 and Figure 5 The secondary filter screen 423, the catalyst filter plate 531, the connecting rod 532 and the mixed flow impeller 6 are made of high temperature resistant and lightweight materials; the elastic modulus of the balance spring 4242 is sufficient to keep the secondary filter screen 423 balanced when no flue gas is introduced. On the one hand, the use of high-temperature resistant and lightweight materials can ensure that the balance spring 4242 can more easily ensure that the secondary filter 423, the catalyst filter plate 531, the connecting rod 532 and the mixed flow impeller 6 are in a balanced state when the flue gas is not introduced; because the secondary filter 423 and the catalyst filter plate 531 will be subject to the rising force of the flue gas, and because the secondary filter 423 and the catalyst filter plate 531 are both provided with fine pores on the surface, the contact area between the secondary filter 423 and the catalyst filter plate 531 and the flue gas is large, and the balance state brought by the balance spring 4242 can be destroyed under the rising force of the flue gas, so that the secondary filter 423 and the catalyst filter plate 531 can both vibrate at high frequency to keep the lower surfaces of the secondary filter 423 and the catalyst filter plate 531 from being blocked, and the secondary filter 423 can ensure that the flue gas entering the denitrification step will not cause damage to the catalyst, and at the same time, the catalyst filter plate 531 can filter out the catalyst escaping with the flue gas, thereby reducing the loss of the catalyst and improving the efficiency of denitrification.

[0051] Working process: the flue gas enters the shell 41 through the air intake pipe 1 and swirls downward to separate solid particles and oily particles from the flue gas by centrifugal force. When the flue gas reaches the bottom of the shell 41, negative pressure is formed in the inner circle, thereby rotating inward and rising. The flue gas passes through the secondary filter 423, causing the secondary filter 423 to shake and filter for a second time. The filtered particulate matter enters the outer circle of the flue gas again under the action of the inward centrifugal force and is separated by the centrifugal force of the outer circle; ammonia enters the ammonia channel 2. When ammonia reaches the bottom of the laminar flow reactor 5, negative pressure is formed in the inner circle, which rotates inward and rises in the opposite direction to the direction of rotation of the flue gas. The inward rotation and rise of ammonia drives the mixed flow impeller 6 to rotate. The rotation of the mixed flow impeller 6 makes the ammonia and the flue gas fully mixed and flows to the catalytic bed 523 with an upward centrifugal diffusion motion trend for denitrification reaction. The flue gas that has completed denitrification flows to the desulfurization reactor 7. During the process, the catalyst filter plate 531 filters out the escaped catalyst carried in the flue gas.

[0052] Specifically, flue gas is introduced from the air intake duct 1 in a tangential direction to the upper cylindrical direction of the shell 41, and under the guidance of the upper cylindrical structure of the shell 41 and the lower conical structure, it performs a spiral downward motion. During the flow, the internal particles are thrown onto the inner wall by centrifugal force and fall along the inner wall to the dust storage chamber 43 under the action of the airflow, and the adsorption plate 44 rotates under the action of the flue gas rotating in the outer circle to capture the oily particles. After the oily particles are gathered in the oil gathering space 443, they will flow from the oil-repellent channel 442 to the bottom of the shell 41, thereby ensuring that the oily particles can be quickly separated and preventing the oily particles in the flue gas from causing damage to the catalyst. When the flue gas reaches the bottom of the inverted cone structure, the outward-rotating flue gas is restricted by the inner wall of the inverted cone structure and the particles in the rotating flue gas under the action of centrifugal force are pushed to the inner wall of the shell 41, resulting in a decrease in the air density in the central area, forming a negative pressure at the center of the cone bottom. The pressure zone causes the flue gas reaching the bottom of the inverted cone structure to change direction under the action of the negative pressure zone and the inner wall of the bottom of the inverted cone structure, forming an inwardly rotating rising airflow, so that the flue gas that has completed dust removal rises and flows out; in order to prevent the rising inwardly rotating flue gas from carrying tiny oily particles, when the inwardly rotating flue gas rises to the position of the secondary filter screen 423, the rising force will destroy the equilibrium state when the rising flue gas contacts the secondary filter screen 423, and because the flow rate of the rising flue gas is changing all the time, the rising force generated is also changing all the time. At this time, the secondary filter screen 423 continues to vibrate at a high frequency under the change of the rising force, so that the filtered particles cannot adhere to the secondary filter screen 423, and because the rising flue gas in the inner circle is rotating and rising, the particles that cannot adhere to the secondary filter screen 423 will be thrown to the outer circle by the centrifugal force, and when it reaches the outward rotating sinking flue gas position of the outer circle, it will be thrown to the inner wall of the shell 41 by the centrifugal force for sedimentation;

[0053] Ammonia is introduced from the ammonia channel 2 in a direction tangential to the mixing chamber 511, and the direction of ammonia introduction is opposite to that of flue gas introduction. Ammonia acts on the inner wall of the mixing chamber 511 to perform a similar movement to that of flue gas (only the spiral direction is opposite); after the ammonia rises inwardly, its rising force and spiral force drive the mixed flow impeller 6 to rotate, and the mixed flow impeller 6 rotates to mix the rising flue gas in the rising channel 42 and the ammonia forming the inward rotation. Since the rotation directions of ammonia and flue gas are opposite, the mixing uniformity will be improved at this time; and the blades of the mixed flow impeller 6 are of a mixed flow structure, which can combine the advantages of axial flow fans and centrifugal fans, and cooperate with the inverted cone structure of the mixing tube 512 to achieve mixing of ammonia and flue gas while entering the catalyst layer 52 with the trend of axial flow diffusion, completing the pre-distribution of the mixed gas of ammonia and flue gas, so that it can fully contact with the catalyst, thereby improving the denitration efficiency;

[0054] When the denitrification reaction is completed, the flue gas that has completed denitrification will carry a small amount of catalyst to escape. Since the catalyst filter plate 531 and the secondary filter screen 423 are connected, when the secondary filter screen 423 vibrates, the catalyst filter plate 531 will also be deformed under the pull of the connecting rod 532. Since the catalyst filter plate 531 is an elastic metal plate, when it is deformed, it forms a force in a relative direction with the rising force of the flue gas under its own restoring force, so that the catalyst filter plate 531 vibrates at a high frequency to avoid clogging of the catalyst filter plate 531, thereby reducing catalyst loss and further ensuring denitrification efficiency. The flue gas after passing through the catalyst filter plate 531 flows into the desulfurization reactor 7 for desulfurization reaction.

[0055] The above shows and describes the basic principles, main features and advantages of the present invention. Those skilled in the art should understand that the present invention is not limited to the above embodiments, and the above embodiments and descriptions are only for explaining the principles of the present invention. Without departing from the spirit and scope of the present invention, the present invention may have various changes and improvements, which fall within the scope of the present invention to be protected, and the scope of the present invention to be protected is defined by the attached claims and their equivalents.

Claims

1. A flue gas desulfurization, denitrification and dust removal separation device, comprising an air inlet pipe (1), an ammonia channel (2) and an air outlet channel (3); characterized in that: The invention also comprises a separation mechanism (4), a laminar flow reactor (5), a mixed flow impeller (6) and a desulfurization reactor (7); the separation mechanism (4) is connected to the air intake pipe (1); the laminar flow reactor (5) is connected to the separation mechanism (4); the mixed flow impeller (6) is connected between the separation mechanism (4) and the laminar flow reactor (5); the desulfurization reactor (7) is connected to the laminar flow reactor (5); the flue gas enters the separation mechanism (4) through the air intake pipe (1) and performs downward swirling flow, thereby utilizing centrifugal force to separate solid particles and oily particles from the flue gas. When the flue gas reaches the bottom of the separation mechanism (4), negative pressure is formed in the inner circle, so that the flue gas rotates inward and rises; ammonia enters the laminar flow reactor (5) from the ammonia channel (2) and rotates downward. When the ammonia reaches the bottom of the laminar flow reactor (5), negative pressure is formed in the inner circle, so that the flue gas rotates inward and rises in a direction opposite to the direction of rotation of the flue gas. The inward rotation and rise of the ammonia drives the mixed flow impeller (6) to rotate. The rotation of the mixed flow impeller (6) allows the ammonia and flue gas to be fully mixed and enter the upper layer of the laminar flow reactor (5) with an upward movement trend. The upward force of the ammonia and flue gas drives the separation mechanism (4) to vibrate.

2. The flue gas desulfurization, denitrification and dust removal separation equipment according to claim 1 is characterized in that: The separation mechanism (4) comprises a shell (41), an ascending channel (42), a dust storage chamber (43) and an adsorption plate (44); the shell (41) is connected to the air intake duct (1); the upper portion of the shell (41) is a cylindrical structure, the lower portion is an inverted cone structure, and the air intake duct (1) is tangentially connected to the upper cylindrical structure; the ascending channel (42) is arranged at the center position inside the shell (41); the dust storage chamber (43) and the shell (41) are arranged at the lower portion; and the adsorption plate (44) is rotatably mounted on the inner wall of the shell (41).

3. A flue gas desulfurization, denitrification and dust removal separation equipment according to claim 2, characterized in that: The adsorption plate (44) is provided with an adsorption hole (441) on its surface, and an oil-repellent channel (442) and an oil-collecting space (443) are provided inside; the adsorption hole (441) is an inverted cone structure, and the end with a larger hole diameter faces the outside of the adsorption plate (44).

4. The flue gas desulfurization, denitrification and dust removal separation equipment according to claim 2 is characterized in that: The ascending channel (42) comprises a tube body (421), a filter chute (422), a secondary filter (423) and an oscillation spring (424); the tube body (421) is connected to the laminar flow reactor (5); the filter chute (422) is arranged at the lower part of the tube body (421); the secondary filter (423) is slidably installed in the filter chute (422), and the secondary filter (423) is a rigid structure; the oscillation spring (424) is connected to the secondary filter (423).

5. The flue gas desulfurization, denitrification and dust removal separation equipment according to claim 4 is characterized in that: The edge of the secondary filter (423) is provided with a sealing ring (4231); the vibration spring (424) includes a vibration spring (4241) and a balance spring (4242); the vibration springs (4241) are installed in a circular array above the edge of the secondary filter (423); and the balance springs (4242) are installed in a circular array with the same number below the edge of the secondary filter (423).

6. The flue gas desulfurization, denitrification and dust removal separation equipment according to claim 2, characterized in that: The laminar flow reactor (5) comprises an ammonia mixing layer (51), a catalytic layer (52) and an outflow layer (53); the ammonia mixing layer (51) comprises a mixing chamber (511) and a mixing tube (512); the lower part of the mixing chamber (511) is connected to the ascending channel (42); the upper part of the inner wall of the mixing chamber (511) is a cylindrical structure, and the lower part is an inverted cone structure, and the ammonia channel (2) is tangentially connected to the mixing chamber (511); the mixing tube ( The catalyst layer (52) comprises an inverted cone section (521), a fine porous plate (522) and a catalyst bed (523); the inverted cone section (521) is connected to the ammonia mixing layer (51); the fine porous plate (522) is connected to the inverted cone section (521); the catalyst bed (523) is arranged on the upper side of the fine porous plate (522); and the outflow layer (53) is arranged on the upper end of the catalyst layer (52).

7. The flue gas desulfurization, denitrification and dust removal separation equipment according to claim 6, characterized in that: The mixing tube (512) is of an inverted cone structure; the axis of the mixed flow impeller (6) coincides with the axes of the ascending channel (42) and the mixing tube (512); the radius R1 of the mixed flow impeller (6) is slightly smaller than the radius R2 of the bottom of the mixing tube (512) and larger than the radius R3 of the ascending channel (42); and the horizontal plane where the upper end surface of the mixed flow impeller (6) is located is higher than the horizontal plane where the lowest end of the mixing tube (512) is located.

8. The flue gas desulfurization, denitrification and dust removal separation equipment according to claim 6, characterized in that: The vertical plane where the tangent line between the air intake pipe (1) and the shell (41) lies and the vertical plane where the tangent line between the ammonia passage (2) and the mixing chamber (511) lies are the same vertical plane, and the air intake directions of the two are opposite.

9. The flue gas desulfurization, denitrification and dust removal separation equipment according to claim 6, characterized in that: The outflow layer (53) comprises a catalyst filter plate (531) and a connecting rod (532); the catalyst filter plate (531) is arranged on the top of the catalytic layer (52), and the catalyst filter plate (531) is an elastic metal thin plate with pores smaller than the catalyst particle size; the connecting rod (532) is connected between the catalyst filter plate (531) and the secondary filter screen (423), and passes through the pore plate (522).

10. The flue gas desulfurization, denitrification and dust removal separation equipment according to claim 9, characterized in that: The secondary filter screen (423), the catalyst filter plate (531), the connecting rod (532) and the mixed flow impeller (6) are made of high temperature resistant and lightweight materials; the elastic modulus of the balance spring (4242) is sufficient to enable the secondary filter screen (423) to maintain balance when no flue gas is introduced.

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