KR102382875B1 - Desulfurization, denitrification and ammonia removal system - Google Patents

Abstract

A desulfurization, denitrification and ammonia removal system is provided. The system includes an adsorption tower, a cracking tower, a distributor, a first activated carbon conveyor, and a second activated carbon conveyor. A flue gas inlet is provided on one side of the adsorption tower. A flue gas outlet is provided on another side of the adsorption tower. The adsorption cavity and the ammonia removal cavity are provided inside the adsorption tower. An adsorption cavity is provided on the side close to the flue gas inlet. An ammonia removal cavity is provided on the side close to the flue gas outlet. A first activated carbon conveyor is connected to the material outlet of the adsorption tower and the material inlet of the distributor. A second activated carbon conveyor is connected to the material outlet of the cracking tower and the material inlet of the adsorption cavity. The material outlet of the distributor is connected to the material inlet of the ammonia removal cavity and the material inlet of the cracking tower, respectively. This application divides the adsorption tower into two functional areas, the adsorption reaction cavity implements the functions of desulfurization, denitrification and dust removal, and the ammonia removal cavity is filled with fresh activated carbon or acid activated carbon from the flue gas passing through the adsorption reaction bed By trapping ammonia, the function of effectively preventing the release of ammonia from the outlet is realized.

Description

Desulfurization, denitrification and ammonia removal system

This application claims priority to Chinese Patent Application No. 201810306592.8, entitled "Desulfurization, Denitrification and Ammonia Removal System", filed with the Chinese Patent Office on April 8, 2018, the entirety of which is incorporated herein by reference. .

The present invention relates to flue gas purification using activated carbon, which belongs to a flue gas purification device using activated carbon and suitable for air pollution treatment, in particular, a desulfurization, denitrification and ammonia removal system for sintering flue gas purification. It relates to devices, and to the field of environmental protection.

For industrial flue gases, in particular flue gases from sintering machines in the iron and steel industry, it is ideal to use desulfurization and denitrification units comprising activated carbon adsorption towers and denitration towers and corresponding processes. In a desulfurization and denitration unit comprising an activated carbon adsorption tower and a desorption tower (or regeneration tower), the activated carbon adsorption tower removes sulfur oxides, nitrogen oxides and dioxins from sinter flue gas or exhaust gas (especially flue gas from sintering machines in the iron and steel industry). While it is used to adsorb the pollutants it contains, the desorption tower is used for thermal regeneration of activated carbon.

Desulfurization using activated carbon has a high desulfurization rate and at the same time can realize denitrification, dioxin removal and dust removal, and has the advantages of no wastewater and no residue, which is a very promising method for flue gas purification. Activated carbon can be regenerated at high temperatures. At temperatures above 350° C., pollutants such as sulfur oxides, nitrogen oxides and dioxins adsorbed by the activated carbon are rapidly desorbed or decomposed (sulfur dioxide is desorbed, nitrogen oxides and dioxins are decomposed). In addition, as the temperature rises, the regeneration rate of the activated carbon is further accelerated and the regeneration time is shortened. Preferably, the regeneration temperature of the activated carbon in the desorption tower is controlled to be approximately 430 °C. Accordingly, the ideal desorption temperature (or regeneration temperature) is, for example, in the range of 390 to 450°C, more preferably 400 to 440°C.

The role of the desorption tower is to release the SO ₂ adsorbed by the activated carbon. During residence for a certain period of time at a temperature of 400 ° C. or higher, dioxins can be decomposed by 80% or more. Activated carbon can be reused after cooling and sieving. The released SO ₂ can be used to produce sulfuric acid and the like. The desorbed activated carbon is transferred to an adsorption tower through a transfer device and reused to adsorb SO ₂ and NO _X .

NO _X and ammonia react with SCR and SNCR in an adsorption tower and a desorption tower to remove NO _X. The dust is adsorbed by the activated carbon as it passes through the adsorption tower, and is sieved by a vibration sieve at the bottom of the desorption tower, and the activated carbon powder under the sieve is sent to the ash vessel.

In the prior art, ammonia is injected directly into the flue gas inlet following a flue gas purification process using activated carbon. To increase the denitrification rate, the amount of ammonia injected into the flue gas inlet is generally increased, but at the same time ammonia emissions from the outlet are more severe.

In addition, the dust is adsorbed to the activated carbon when passing through the adsorption tower, sieved by a vibrating sieve at the bottom of the desorption tower, and the activated carbon powder under the sieve is sent to the ash container, and the activated carbon powder remaining on the sieve is recyclable. is considered At present, a sieve commonly used is a sieve with a square hole, and the side length (a) of each square hole is determined according to the sieving requirements, and is generally about 1.2 mm. However, a substantially tablet-shaped activated carbon with dimensions of φ 9 mm x 1 mm would be considered recyclable when sieved by such a sieve. Tablet-shaped activated carbon has low abrasion resistance and low compressive strength, and is easy to break after entering the flue gas purification system. On the one hand, the resistance of the flue gas purification system is increased due to more powder in the activated carbon bed, which increases the operating cost of the system; On the other hand, the risk of high-temperature combustion of the activated carbon is increased. In addition, the dust in the outlet flue gas mainly comprises some fine particles carried in the original flue gas and freshly entrained activated carbon powder when the flue gas passes through the activated carbon bed, and a large amount of the activated carbon bed powder is dust at the flue gas outlet will affect the surrounding environment and cause air pollution.

In addition, the activated carbon discharging apparatus in the prior art includes a circular roller feeder and a feed rotary valve, as shown in FIG. 10 .

First of all, in the case of the circular roller feeder, during operation, the activated carbon moves downward by the action of gravity under the control of the circular roller feeder. The different rotational speeds of the circular roller feeder determine the moving speed of the activated carbon. Activated carbon discharged from the circular roller feeder enters the feed rotary valve, is discharged, and then enters the conveying device for recirculation. The main function of the feed rotary valve is to keep the adsorption tower sealed during discharge, thereby preventing harmful gases in the adsorption tower from leaking into the air.

Because the flue gas contains a certain amount of water vapor and dust, during the adsorption process a small amount of activated carbon will stick to each other and form a block blocking the effluent outlet as shown in FIG. If the discharge outlet is severely clogged, the activated carbon cannot move continuously, which may lead to the loss of adsorption saturation and purification effect of the activated carbon, and the temperature of the activated carbon bed may increase due to the heat storage of the activated carbon, thereby increasing the potential safety risk. Current processing methods manually remove blocks after the system is shut down. In addition, during the production process, round roller feeders often suffer from defects such as material leaking when flue gas pressure changes, material loss during shutdown, and the like. In addition, the large number of round roller feeders (every time one fails, the entire large unit must be shut down), expensive, and difficult to maintain and repair, places some limitations on the development of activated carbon technology.

Second, in the case of the feed rotary valve of the prior art, the problem is as follows. In order to transport fragile particles such as desulfurization and denitrification activated carbon, rotary valves are used on the one hand to ensure the airtightness of the tower body and on the other hand to achieve non-destructive material transport. However, if the conveying medium is sheared due to the rotation of the blades during the rotary valve conveying process, as shown in FIG. 10 , the cost of operating the system will increase. In addition, the shear phenomenon causes the valve body to wear out, airtightness is reduced, and the service life is shortened. In particular, when the supply port is filled with material, the shear effect of the blade and valve housing on the conveying medium while the valve core rotates is more evident. Generally, for large adsorption towers with a height of about 20 meters, if the round roller feeder or rotary valve fails during the production process, the adsorption tower is filled with a large amount of activated carbon, and manual removal and maintenance or reinstallation are very difficult, and operation The continuous operation of the process will suffer great losses because the impact and losses caused by the shutdown are unimaginable.

To avoid escape of excess ammonia, according to the present disclosure, the adsorption tower captures ammonia in two functional areas: an adsorption reaction chamber that performs functions such as desulfurization, denitrification and dust removal, and a flue gas passing through the adsorption reaction bed. Thus, it is divided into an ammonia removal chamber filled with fresh activated carbon or acid activated carbon to effectively prevent ammonia escape at the outlet.

According to a first aspect provided by the present disclosure, a desulfurization, denitrification and ammonia removal system is provided.

The system includes an adsorption tower, a desorption tower, a distributor, a first activated carbon conveyor and a second activated carbon conveyor. A flue gas inlet (A) is provided on one side of the adsorption tower. A flue gas outlet (B) is provided on another side of the adsorption tower. The adsorption chamber and the ammonia removal chamber are provided inside the adsorption tower. The adsorption chamber and the ammonia removal chamber are disposed perpendicularly and parallel to the adsorption tower. The adsorption chamber is arranged on the side close to the flue gas inlet (A). The ammonia removal chamber is arranged on the side close to the flue gas outlet (B). The first activated carbon conveyor is connected to the outlet port of the adsorption tower and the feed port of the distributor. A second activated carbon conveyor is connected to the outlet port of the desorption tower and the feed port of the adsorption chamber. The outlet port of the distributor is connected to the feed port of the ammonia removal chamber and the feed port of the desorption tower.

Preferably, the flue is provided downstream of the flue gas inlet (A). The flue downstream of the flue gas inlet A is divided into two layers, the flue upper part and the flue lower part, respectively. An ammonia gas blowing device is provided at the upper end of the flue.

According to the present disclosure, a porous plate is provided between the adsorption chamber and the ammonia removal chamber. The adsorption chamber is separated from the ammonia removal chamber by a porous plate.

Preferably, a vibration sieve is provided below the outlet port of the desorption tower. The front part of the second activated carbon conveyor is connected to the discharge port of the vibrating sieve.

Preferably, the thickness of the adsorption chamber is 1 to 10 times, preferably 2 to 8 times, more preferably 3 to 5 times the thickness of the ammonia removal chamber.

Preferably, the distributor is provided with a sieve device, a large particle activated carbon outlet and a particulate activated carbon outlet. A large particle activated carbon outlet is disposed above the sieve device. A particulate activated carbon outlet is disposed below the sieve device. A large particle activated carbon outlet is connected to the supply port of the ammonia removal chamber. The particulate activated carbon outlet is connected to the feed port of the desorption tower. Preferably, the sieve device provided in the dispenser is provided with a sieve having a rectangular mesh, wherein the length L of each rectangular mesh is at least 3D, and the width a of each rectangular mesh is 0.65 h to 0.95 h (preferably 0.7 h) to 0.9 h, more preferably 0.73 h to 0.85 h), where D is the diameter of the circular cross-section of the activated carbon cylinder held on the sieve, and h is the minimum length of the granular activated carbon cylinder held on the sieve.

In particular, in order to overcome the technical problems encountered in the desulfurization and denitration apparatus of the present invention, the minimum length (h) of the activated carbon cylinder should generally be 1.5 mm to 7 mm. For example, h = 2 mm, 4 mm or 6 mm.

D (or φ) depends on the specific requirements of the desulphurization and denitrification unit. In general, D (or φ) = 4.5 mm to 9.5 mm, preferably 5 mm to 9 mm, more preferably 5.5 mm to 8.5 mm, even more preferably 6 mm to 8 mm, for example 6.5 mm , 7 mm, or 7.5 mm.

According to a second aspect provided by the present disclosure, a desulfurization, denitrification and ammonia removal system is provided.

The system includes an adsorption tower, a desorption tower, first and second activated carbon conveyors, and a storage vessel. A flue gas inlet (A) is provided on one side of the adsorption tower. A flue gas outlet (B) is provided on another side of the adsorption tower. The adsorption chamber and the ammonia removal chamber are provided inside the adsorption tower. The adsorption chamber and the ammonia removal chamber are disposed perpendicularly and parallel to the adsorption tower. The adsorption chamber is arranged on the side close to the flue gas inlet (A). The ammonia removal chamber is arranged on the side close to the flue gas outlet (B). The first activated carbon conveyor is connected to the outlet port of the adsorption tower and the feed port of the desorption tower. A second activated carbon conveyor is connected to the outlet port of the desorption tower and the feed port of the adsorption chamber.

Such systems further include an SO ₂ recovery system, a sulfur-rich gas delivery pipeline, and an SO ₂ recovery system tail gas delivery pipeline. One end of the sulfur-rich gas delivery pipeline is connected to a desorption tower. The other end of the sulfur-rich gas delivery pipeline is connected to the gas inlet of the SO ₂ recovery system. One end of the SO ₂ recovery system tail gas delivery pipeline is connected to the gas outlet of the SO ₂ recovery system. The other end of the SO ₂ recovery system tail gas delivery pipeline is connected to the gas inlet of the storage vessel. The gas outlet of the storage vessel is connected to the flue gas outlet (B).

Optionally, the tail end of the second activated carbon conveyor is further connected to the supply port of the storage vessel, and the discharge port of the storage vessel is connected to the supply port of the ammonia removal chamber.

Preferably, the flue is provided downstream of the flue gas inlet (A). The flue downstream of the flue gas inlet A is divided into two layers, the flue upper part and the flue lower part, respectively. An ammonia gas blowing device is provided at the upper end of the flue.

According to the present disclosure, a porous plate is provided between the adsorption chamber and the ammonia removal chamber. The adsorption chamber is separated from the ammonia removal chamber by a porous plate.

Preferably, a vibrating sieve is provided below the discharge port of the desorption tower. The front part of the second activated carbon conveyor is connected to the discharge port of the vibrating sieve.

Preferably, the thickness of the adsorption chamber is 1 to 10 times, preferably 2 to 8 times, more preferably 3 to 5 times the thickness of the ammonia removal chamber.

According to a third aspect provided by the present disclosure, a desulfurization, denitrification and ammonia removal system is provided.

The system includes an adsorption tower, a desorption tower, first and second activated carbon conveyors, and a storage vessel. A flue gas inlet (A) is provided on one side of the adsorption tower. A flue gas outlet (B) is provided on another side of the adsorption tower. The adsorption chamber and the ammonia removal chamber are provided inside the adsorption tower. The adsorption chamber and the ammonia removal chamber are disposed perpendicularly and parallel to the adsorption tower. The adsorption chamber is arranged on the side close to the flue gas inlet (A). The ammonia removal chamber is arranged on the side close to the flue gas outlet (B). The first activated carbon conveyor is connected to the outlet port of the adsorption tower and the feed port of the desorption tower. A second activated carbon conveyor is connected to the outlet port of the desorption tower and the feed port of the adsorption chamber.

The system includes a raw flue gas branch and a raw flue gas recirculation transport pipeline. One end of the raw flue gas branch is connected to the front of the flue gas inlet A. The other end of the raw flue gas branch is connected to the gas inlet of the storage vessel. The gas outlet of the storage vessel is connected to the rear of the flue gas inlet A via a raw flue gas recirculation transport pipeline.

Optionally, the tail end of the second activated carbon conveyor is also connected to the supply port of the storage vessel, and the discharge port of the storage vessel is connected to the supply port of the ammonia removal chamber.

Preferably, the flue is provided downstream of the flue gas inlet (A). The flue downstream of the flue gas inlet A is divided into two layers, the flue upper part and the flue lower part, respectively. An ammonia gas blowing device is provided at the upper end of the flue.

Preferably, an ammonia gas blowing device is provided downstream of the flue gas at the connection point of the raw flue gas branch and the flue gas inlet (A).

According to the present disclosure, a porous plate is provided between the adsorption chamber and the ammonia removal chamber. The adsorption chamber is separated from the ammonia removal chamber by a porous plate.

Preferably, a vibrating sieve is provided below the discharge port of the desorption tower. The front part of the second activated carbon conveyor is connected to the discharge port of the vibrating sieve.

Preferably, the thickness of the adsorption chamber is 1 to 10 times, preferably 2 to 8 times, more preferably 3 to 5 times the thickness of the ammonia removal chamber.

In the present disclosure, according to a first embodiment, activated carbon having adsorbed flue gas at the bottom of the adsorption tower is used as an activated carbon bed in the ammonia removal chamber. The inlet flue of the adsorption tower is divided into two layers: an upper layer and a lower layer. Ammonia gas is injected into the upper layer to achieve flue gas desulfurization and denitrification. The activated carbon in the upper layer of the adsorption tower is moved downward by gravity to the lower layer of the adsorption tower. The gas at the bottom of the flue is mainly acid gas, and the activated carbon absorbs acid gas such as SO ₂ to achieve acidification in the bottom layer of the adsorption tower. After being discharged from the adsorption tower, the activated carbon is transferred to a distributor through a conveyor, a part of the activated carbon in the distributor flows into the ammonia removal bed, and a part of the activated carbon is regenerated in the desorption tower. Preferably, the distributor has a particle size distribution function, which allows the large particle activated carbon to enter the ammonia removal bed and the particulate activated carbon and dust to flow into the desorption tower.

In the present disclosure, according to the second embodiment, acidification of the raw material (ie, fresh activated carbon/regenerated activated carbon) is achieved by using an acid-produced tail gas. The acid-produced tail gas contains a certain amount of SO ₂ gas, the concentration of which is controllable according to the requirements, typically 200 mg/Nm3 to 600 mg/Nm3. This tail gas is transferred to a fresh activated carbon vessel or a regenerated activated carbon vessel to achieve acidification of the activated carbon, then the tail gas is returned to the exhaust flue of the adsorption tower, and the acidified activated carbon is introduced into the ammonia removal chamber. This method simultaneously achieves purification of acid-produced tail gas and recycling of resources.

In the present disclosure, according to a third embodiment, acidification of the raw material (ie, fresh activated carbon/regenerated activated carbon) is achieved by using an acidic substance in the raw flue gas. The raw flue gas contains a certain amount of acid gas. A part of the flue gas before ammonia injection is transferred to a fresh activated carbon vessel or a regenerated activated carbon vessel to achieve acidification of the activated carbon, then the flue gas is returned to the inlet flue of the adsorption tower, and the acidified activated carbon is introduced into the ammonia removal chamber.

According to the present disclosure, the adsorption chamber and the ammonia removal chamber are two chambers, both of which are layers of activated carbon. The activated carbon in the adsorption chamber is fresh or regenerated activated carbon; Activated carbon in the ammonia removal chamber is activated carbon adsorbed with untreated flue gas, or fresh or regenerated activated carbon treated with tail gas of SO ₂ recovery system.

According to the present disclosure, the evacuation port of the adsorption tower includes an evacuation port of the adsorption chamber and an evacuation port of the ammonia removal chamber. The discharge port of the adsorption chamber and the discharge port of the ammonia removal chamber may be respectively connected to the first activated carbon conveyor. Alternatively, after the exhaust port of the adsorption chamber and the exhaust port of the ammonia removal chamber are combined, the entire exhaust port is connected to the first activated carbon conveyor.

According to the present disclosure, downstream of the flue gas inlet A refers to the direction in which the flue gas flows, ie the direction downstream of the flue gas inlet.

According to the present disclosure, the thickness of the adsorption chamber and the thickness of the ammonia removal chamber are not particularly required, which are determined according to the actual production process. In general, the thickness of the adsorption chamber is 1 to 10 times, preferably 2 to 8 times, more preferably 3 to 5 times the thickness of the ammonia removal chamber.

According to the present disclosure, when the tail end of the second activated carbon conveyor is connected to the supply port of the storage vessel, the discharge port of the storage vessel is connected to the supply port of the ammonia removal chamber. When the tail end of the second activated carbon conveyor is connected only to the supply port of the adsorption chamber, the supply port of the storage vessel is connected to the new activated carbon vessel. The discharge port of the storage vessel is connected to the supply port of the ammonia removal chamber.

According to the present disclosure, the tail end of the second activated carbon conveyor is set according to the progress direction of the transport of the activated carbon, and the tail end of the second activated carbon conveyor is the position at which the transport of the activated carbon on the second activated carbon conveyor ends (the position where the transport distance is long) am.

In the present disclosure, depending on the flow path and direction of the flue gas, the location that enters the flue gas inlet is in front of the flue gas inlet (away from the adsorption tower), and the location close to the adsorption tower is the rear of the flue gas inlet.

In all desulfurization and denitration systems of the present disclosure, a vibrating sieve equipped with a sieve is generally provided below the discharge port at the bottom of the desorption tower or provided downstream of the desorption tower.

In order to avoid the tablet-shaped activated carbon being retained on the sieve, a sieve having a rectangular mesh or a strip mesh is designed in the present disclosure. The sieve can be mounted on the vibrating sieve to sieve the activated carbon particles that meet the requirements of the desulfurization and denitration apparatus.

Accordingly, preferably, a sieve having a rectangular mesh or a strip mesh is provided, wherein the length of each rectangular mesh is L≧3D, and the width of each rectangular mesh is a = 0.65h to 0.95h (preferably 0.7h) to 0.9 h, more preferably 0.73 h to 0.85 h), where D is the diameter of the circular cross-section of the activated carbon cylinder held on the sieve, and h is the minimum length of the granular activated carbon cylinder held on the sieve.

In particular, in order to overcome the technical problems encountered in the desulfurization and denitration apparatus of the present invention, the minimum length (h) of the activated carbon cylinder should generally be 1.5 mm to 7 mm. For example, h = 2 mm, 4 mm or 6 mm.

D (or φ) depends on the specific requirements of the desulphurization and denitrification unit. In general, D (or φ) = 4.5 mm to 9.5 mm, preferably 5 mm to 9 mm, more preferably 5.5 mm to 8.5 mm, even more preferably 6 mm to 8 mm, for example 6.5 mm , 7 mm, or 7.5 mm.

Adsorption towers generally have two or more activated carbon feed chambers.

Preferably, a circular roller feeder or discharge circular roller G is provided at the bottom of each activated carbon supply chamber of the adsorption tower. In the case of the discharging circular roller G described herein, a discharging circular roller of the prior art may be used. However, preferably, instead of the circular roller feeder or discharge circular roller G, a star-wheel type activated carbon discharging device G can be used, which includes a front baffle in the lower part of the activated carbon feeding chamber and a rear baffle, and a star-wheel-type activated carbon discharge roller located below the discharge port formed by the front and rear baffles and two side plates at the lower portion of the activated carbon supply chamber. A star-wheel type activated carbon discharge roller includes a circular roller and a plurality of blades distributed conformally or substantially conformally along a circumference of the circular roller. More specifically, a star-wheel type activated carbon discharge roller is used under the discharge port formed by the front and rear baffles and two side plates in the lower part of the activated carbon supply chamber.

When viewed from the cross section of the star-wheel type activated carbon discharging roller, the star-wheel type activated carbon discharging roller exhibits a star-wheel configuration or shape.

The star-wheel type activated carbon discharging device mainly includes a front baffle and a rear baffle and two side plates of the activated carbon discharging port, a blade and a circular roller. The front baffle and the rear baffle are fixedly disposed, and the activated carbon exhaust passage, ie, the exhaust port, is between the front baffle and the rear baffle. The exhaust port includes a front baffle, a rear baffle and two side plates. A circular roller is disposed at the lower end of the front baffle and at the lower end of the rear baffle. The blades are uniformly distributed and fixed on a circular roller. The circular roller is rotated by a motor, and the direction of rotation is from the rear baffle to the front baffle. The included angle or spacing between adjacent blades should not be too large. The included angle θ between adjacent blades is generally less than 64°, for example 12° to 64°, preferably 15° to 60°, preferably 20° to 55°, more preferably 25° to 50°, even more preferably 30° to 45°. A gap or distance s is provided between the blade and the bottom of the rear baffle. s is generally from 0.5 mm to 5 mm, preferably from 0.7 mm to 3 mm, more preferably from 1 mm to 2 mm.

The radius of the outer circumference of the star-wheel-type activated carbon discharging roller (or the radius of rotation of the outer circumference of the blade on the circular roller) is r. r is equal to the radius of the cross section (circle) of the circular roller 106a plus the width of each blade.

In general, the radius of the cross section (circle) of the circular roller is 30 mm to 120 mm, preferably 50 mm to 100 mm, and the width of each blade is 40 mm to 130 mm, preferably 60 mm to 100 mm.

The distance between the center of the circular roller and the bottom of the front baffle is h. h is generally larger than r + (12 to 30)mm and smaller than r/sin58°, which can ensure that the activated carbon is discharged smoothly and that the activated carbon does not slide by itself when the circular roller is not moving.

Generally, in the present disclosure, the cross section of the discharge port of the star-wheel type activated carbon discharging device is a square or rectangle, preferably a rectangle having a length greater than the width, that is, a rectangle having a length greater than the width.

Preferably, the evacuation vessel or bottom vessel (H) of the adsorption tower is provided with one or more evacuation rotary valves.

For the rotary valves described herein, rotary valves of the prior art may be used. Preferably, however, a new type comprising an upper supply port, a valve core, a blade, a valve housing, a lower discharge port, a buffer zone in the upper space of the internal cavity of the valve, and a material-smoothing plate of rotary valves are used. The buffer zone is adjacent to and in communication with the lower space of the supply port, and the length of the cross-section of the buffer zone in the horizontal direction is longer than the length of the cross-section of the supply port in the horizontal direction. The material-smooth plate is disposed in the buffer zone, the upper end of the material-smooth plate is fixed to the upper part of the buffer zone, and the cross section of the material-smooth plate has a "V" shape in the horizontal direction.

Preferably, the cross section of the upper feed port is rectangular and the cross section of the buffer zone is rectangular.

Preferably, the length of the cross-section of the buffer zone is smaller than the length of the cross-section of the blade in the horizontal direction.

Preferably, the material-smooth plate is formed by splicing two single plates, or the material-smooth plate is two plate surfaces bent from one plate.

Preferably, the included angle between two single plates or two plate surfaces is 2α≦120°, preferably 2α≦90°. Accordingly, 2α≦60°, preferably 2α≦45°.

Preferably, the included angle between each single plate or each plate surface and the longitudinal direction of the buffer zone is Φ≧30°, preferably Φ≧45°, more preferably Φ≧the friction angle of the activated carbon material.

Preferably, the bottom of each of the two single plates or the two plate surfaces is arc-shaped.

Preferably, the length of the centerline segment between the two single plates or the two plate surfaces is equal to or less than the width of the cross-section of the buffer zone in the horizontal direction.

Obviously, α + Φ = 90°.

Generally, in the present disclosure, the cross-section of the outlet port of the rotary valve is a square or rectangle, preferably a rectangle having a length greater than the width, that is, a rectangle having a length greater than the width.

In general, the height of the main structure of the adsorption tower is 10 m to 60 m (meter), preferably 12 m to 55 m (meter), preferably 14 m to 50 m, preferably 16 m to 45 m, preferably is 18 m to 40 m, preferably 20 m to 35 m, preferably 22 m to 30 m. The height of the main structure of the adsorption tower refers to the height from the inlet to the outlet of the adsorption tower (main structure). The height of the adsorption tower refers to the height from the activated carbon outlet at the bottom of the adsorption tower to the activated carbon inlet at the top of the adsorption tower, that is, the height of the main structure of the tower.

In general, the desorption tower or the regeneration tower generally has a tower height of from 8 m to 45 m, preferably from 10 m to 40 m, more preferably from 12 m to 35 m. The desorption tower generally has a major cross-sectional area of 6 m ² to 100 m ² , preferably 8 m ² to 50 m ² , more preferably 10 m ² to 30 m ² , even more preferably 15 m ² to 20 m ² .

Also, in the present disclosure, flue gas includes conventional industrial flue gas or industrial exhaust gas in a broad sense.

The thickness of the activated carbon chamber or material chamber refers to the distance or spacing between two porous partition plates of the activated carbon chamber or material chamber.

The present disclosure has the following advantages or advantageous effects.

1. The adsorption tower has two functional areas, namely, an adsorption reaction chamber that performs functions such as desulfurization, denitrification and dust removal, and captures ammonia in the flue gas filled with fresh activated carbon or acid activated carbon and passing through the adsorption reaction bed to achieve denitrification effect It is divided into ammonia removal chamber, which effectively prevents ammonia emission while improving the

2. The porous plate is disposed between the adsorption chamber and the ammonia removal chamber, so that the activated carbon layer of the entire adsorption tower flows clearly into the adsorption chamber and the ammonia removal chamber without obstructing the flow of flue gas.

3. The distributor is equipped with a sieve device, a large particle activated carbon outlet and a particulate activated carbon outlet. The large particle activated carbon outlet is connected to the feed port of the ammonia removal chamber, and the particulate activated carbon outlet is connected to the feed port of the desorption tower. This design ensures the particle size of the activated carbon in the ammonia removal chamber, so that the excess ammonia can be absorbed more effectively.

4. A sieve with a square mesh is used in the vibrating sieve to eliminate the bridging phenomenon of tablet-shaped activated carbon, and to sieve tablet-shaped activated carbon with low abrasion resistance and compressive strength to remove debris and dust in the desulfurization and denitration device. By preventing it, it is possible to reduce the movement resistance of the activated carbon, reduce the risk of high-temperature combustion of the activated carbon in the adsorption tower, and recycle the high-strength activated carbon from the unit.

5. Adopting special discharging device, which reduces the failure of discharging activated carbon, and significantly reduces the downtime and maintenance frequency of the whole device.

1 is a schematic structural diagram of a first design of a desulfurization, denitrification and ammonia removal system according to the present invention;
2 is a schematic structural diagram of a second design of a desulfurization, denitrification and ammonia removal system according to the present invention;
3 is a schematic structural diagram of a third design of the desulfurization, denitrification and ammonia removal system according to the present invention;
4 is a schematic structural diagram of a fourth design of the desulfurization, denitrification and ammonia removal system according to the present invention;
5 is a schematic structural diagram of a fifth design of the desulfurization, denitrification and ammonia removal system according to the present invention;
6 is a schematic structural diagram of a prior art sieve;
7 is a schematic structural diagram of a sieve according to the present invention;
8 is a schematic diagram of activated carbon in tablet form;
9 is a schematic diagram of activated carbon in the form of a strip;
10 and 11 are schematic views of a prior art activated carbon discharging device (circular roller feeder);
12 is a schematic diagram of a star-wheel type activated carbon discharging device according to the present invention;
13 is a schematic diagram of a rotary valve according to the present invention;
14 and 15 are schematic structural diagrams of a cross-section taken along line MM in FIG. 13; and
16 is a schematic structural diagram of a material-smooth plate.

The sinter flue gas to be treated in embodiments is a sinter machine flue gas from the steel industry.

According to a first aspect provided by the present disclosure, a desulfurization, denitrification and ammonia removal system is provided.

The system comprises an adsorption tower (1), a desorption tower (2), a distributor (3), a first activated carbon conveyor (4) and a second activated carbon conveyor (5). The flue gas inlet A is provided on one side of the adsorption tower 1 . The flue gas outlet (B) is provided on another side of the adsorption tower (1). The adsorption chamber 103 and the ammonia removal chamber 104 are provided inside the adsorption tower 1 . The adsorption chamber 103 and the ammonia removal chamber 104 are disposed parallel to the adsorption tower 1 in a vertical direction. The adsorption chamber 103 is arranged on the side close to the flue gas inlet A. The ammonia removal chamber 104 is arranged on the side close to the flue gas outlet B. The first activated carbon conveyor 4 is connected to the discharge port of the adsorption tower 1 and the supply port of the distributor 3 . The second activated carbon conveyor 5 is connected to the discharge port of the desorption tower 2 and the supply port of the adsorption chamber 103 . The outlet port of the distributor 3 is connected to the feed port of the ammonia removal chamber 104 and the feed port of the desorption tower 2 via, for example, a pipe or a chute.

Preferably, the flue is provided downstream of the flue gas inlet (A). The flue downstream of the flue gas inlet A is divided into two layers, the flue upper 101 and the flue lower 102, respectively. The flue top 101 is provided with an ammonia gas blowing device P.

According to the present disclosure, a porous plate 7 is provided between the adsorption chamber 103 and the ammonia removal chamber 104 . The adsorption chamber 103 is separated from the ammonia removal chamber 104 by a porous plate 7 .

Preferably, a vibrating sieve 8 is provided below the discharge port of the desorption tower 2 . The front part of the second activated carbon conveyor 5 is connected to the discharge port of the vibrating sieve 8 .

Preferably, the thickness of the adsorption chamber 103 is 1 to 10 times, preferably 2 to 8 times, more preferably 3 to 5 times the thickness of the ammonia removal chamber 104 .

Preferably, the distributor 3 is provided with a sieve device, a large particle activated carbon outlet and a particulate activated carbon outlet. A large particle activated carbon outlet is disposed above the sieve device. A particulate activated carbon outlet is disposed below the sieve device. A large particle activated carbon outlet is connected to the supply port of the ammonia removal chamber 104 . The particulate activated carbon outlet is connected to the feed port of the desorption tower (2). Preferably, the sieve device provided in the dispenser is provided with a sieve having a rectangular mesh or a strip-shaped mesh (as shown in Figure 7), wherein the length L of each rectangular mesh is at least 3D, and The width a is 0.65 h to 0.95 h (preferably 0.7 h to 0.9 h, more preferably 0.73 h to 0.85 h), where D is the diameter of the circular cross-section of the activated carbon cylinder held on the sieve, and h is the sieve It is the minimum length of granular activated carbon cylinders held on the bed.

In particular, in order to overcome the technical problems encountered in the desulfurization and denitration apparatus of the present invention, the minimum length (h) of the activated carbon cylinder should generally be 1.5 mm to 7 mm. For example, h = 2 mm, 4 mm or 6 mm.

D (or φ) depends on the specific requirements of the desulphurization and denitrification unit. In general, D (or φ) = 4.5 mm to 9.5 mm, preferably 5 mm to 9 mm, more preferably 5.5 mm to 8.5 mm, even more preferably 6 mm to 8 mm, for example 6.5 mm , 7 mm, or 7.5 mm.

According to a second aspect provided by the present disclosure, a desulfurization, denitrification and ammonia removal system is provided.

The system comprises an adsorption tower (1), a desorption tower (2), a first activated carbon conveyor (4) and a second activated carbon conveyor (5), and a storage vessel (6). The flue gas inlet A is provided on one side of the adsorption tower 1 . The flue gas outlet (B) is provided on another side of the adsorption tower (1). The adsorption chamber 103 and the ammonia removal chamber 104 are provided inside the adsorption tower 1 . The adsorption chamber 103 and the ammonia removal chamber 104 are disposed parallel to the adsorption tower 1 in a vertical direction. The adsorption chamber 103 is arranged on the side close to the flue gas inlet A. The ammonia removal chamber 104 is arranged on the side close to the flue gas outlet B. The first activated carbon conveyor 4 is connected to the discharge port of the adsorption tower 1 and the supply port of the desorption tower 2 . The second activated carbon conveyor 5 is connected to the discharge port of the desorption tower 2 and the supply port of the adsorption chamber 103 .

This system further comprises an SO ₂ recovery system (R), a sulfur-rich gas transport pipeline (L1), and an SO ₂ recovery system tail gas transport pipeline (L2). One end of the sulfur-rich gas transport pipeline L1 is connected to a desorption tower 2 . The other end of the sulfur-rich gas delivery pipeline (L1) is connected to the gas inlet of the SO ₂ recovery system (R). One end of the SO ₂ recovery system tail gas delivery pipeline (L2) is connected to the gas outlet of the SO ₂ recovery system (R). The other end of the SO ₂ recovery system tail gas delivery pipeline L2 is connected to the gas inlet of the storage vessel 6 . The gas outlet of the storage vessel 6 is connected to the flue gas outlet B.

Optionally, the tail end of the second activated carbon conveyor 5 is further connected to the supply port of the storage vessel 6 , and the discharge port of the storage vessel 6 is connected to the supply port of the ammonia removal chamber 104 .

Preferably, the flue is provided downstream of the flue gas inlet (A). The flue downstream of the flue gas inlet A is divided into two layers, the flue upper 101 and the flue lower 102, respectively. The flue top 101 is provided with an ammonia gas blowing device P.

According to the present disclosure, a porous plate 7 is provided between the adsorption chamber 103 and the ammonia removal chamber 104 . The adsorption chamber 103 is separated from the ammonia removal chamber 104 by a porous plate 7 .

Preferably, a vibrating sieve 8 is provided below the discharge port of the desorption tower 2 . The front part of the second activated carbon conveyor 5 is connected to the discharge port of the vibrating sieve 8 .

Preferably, the thickness of the adsorption chamber 103 is 1 to 10 times, preferably 2 to 8 times, more preferably 3 to 5 times the thickness of the ammonia removal chamber 104 .

According to a third aspect provided by the present disclosure, a desulfurization, denitrification and ammonia removal system is provided.

The system comprises an adsorption tower (1), a desorption tower (2), a first activated carbon conveyor (4) and a second activated carbon conveyor (5), and a storage vessel (6). The flue gas inlet A is provided on one side of the adsorption tower 1 . The flue gas outlet (B) is provided on another side of the adsorption tower (1). The adsorption chamber 103 and the ammonia removal chamber 104 are provided inside the adsorption tower 1 . The adsorption chamber 103 and the ammonia removal chamber 104 are disposed parallel to the adsorption tower 1 in a vertical direction. The adsorption chamber 103 is arranged on the side close to the flue gas inlet A. The ammonia removal chamber 104 is arranged on the side close to the flue gas outlet B. The first activated carbon conveyor 4 is connected to the discharge port of the adsorption tower 1 and the supply port of the desorption tower 2 . The second activated carbon conveyor 5 is connected to the discharge port of the desorption tower 2 and the supply port of the adsorption chamber 103 .

The system further comprises a raw flue gas branch (L3) and a raw flue gas recirculation transport pipeline (L4). One end of the raw flue gas branch L3 is connected to the front of the flue gas inlet A. The other end of the raw flue gas branch L3 is connected to the gas inlet of the storage vessel 6 . The gas outlet of the storage vessel 6 is connected to the rear of the flue gas inlet A via a raw flue gas recirculation transport pipeline L4.

Optionally, the tail end of the second activated carbon conveyor 5 is also connected to the supply port of the storage vessel 6 , and the discharge port of the storage vessel 6 is connected to the supply port of the ammonia removal chamber 104 .

Preferably, the flue is provided downstream of the flue gas inlet (A). The flue downstream of the flue gas inlet A is divided into two layers, the flue upper 101 and the flue lower 102, respectively. The flue top 101 is provided with an ammonia gas blowing device P.

Preferably, an ammonia gas blowing device P is provided downstream of the flue gas at the connection point of the raw flue gas branch L3 and the flue gas inlet A.

According to the present disclosure, a porous plate 7 is provided between the adsorption chamber 103 and the ammonia removal chamber 104 . The adsorption chamber 103 is separated from the ammonia removal chamber 104 by a porous plate 7 .

Preferably, a vibrating sieve 8 is provided below the discharge port of the desorption tower 2 . The front part of the second activated carbon conveyor 5 is connected to the discharge port of the vibrating sieve 8 .

Preferably, the thickness of the adsorption chamber 103 is 1 to 10 times, preferably 2 to 8 times, more preferably 3 to 5 times the thickness of the ammonia removal chamber 104 .

The sieve device provided in the dispenser is further provided with a sieve having a rectangular mesh or a strip mesh according to the present disclosure, wherein the length L of each rectangular mesh is at least 3D, and the width a of each rectangular mesh is from 0.65h to 0.95h h (preferably 0.7h to 0.9h, more preferably 0.73h to 0.85h), where D is the diameter of the circular cross-section of the activated carbon cylinder held on the sieve, and h is the granular activated carbon held on the sieve This is the minimum length of the cylinder.

In particular, in order to overcome the technical problems encountered in the desulfurization and denitration apparatus of the present invention, the minimum length (h) of the activated carbon cylinder should generally be 1.5 mm to 7 mm. For example, h = 2 mm, 4 mm or 6 mm.

D (or φ) depends on the specific requirements of the desulphurization and denitrification unit. In general, D (or φ) = 4.5 mm to 9.5 mm, preferably 5 mm to 9 mm, more preferably 5.5 mm to 8.5 mm, even more preferably 6 mm to 8 mm, for example 6.5 mm , 7 mm, or 7.5 mm.

Embodiment A

As shown in FIG. 7, when the size (holding size of the sieve) of the final activated carbon to be recycled in the desulfurization and denitrification device should be φ9 mm (diameter, D) x 6 mm (length, h), the sieve is subjected to a vibrating sieve ( 3) It is designed to be used in monolayers. The width (a) and length (L) of each rectangular mesh is 5 mm (width, a) x 27 mm (length, L). D is the diameter of the circular cross-section of the activated carbon cylinder to be held on the sieve, and h is the minimum length of the granular activated carbon cylinder to be held on the sieve. a = 0.833 h.

Embodiment B

7, when the size (holding size of the sieve) of the final activated carbon to be recycled in the desulfurization and denitration device should be φ8 mm (diameter, D) x 4 mm (length, h), the sieve is subjected to a vibrating sieve ( 3) It is designed to be used in monolayers. The width (a) and length (L) of each rectangular mesh is 3 mm (width, a) x 27 mm (length, L). D is the diameter of the circular cross-section of the granular activated carbon cylinder to be held on the sieve. a = 0.75 h. These sieves with this mesh size are used to hold medium-sized activated carbon.

Embodiment C

7, when the size of the final activated carbon to be recycled in the desulfurization and denitration apparatus (retaining size of the sieve) should be φ5 mm (diameter, D) x 2 mm (average length), the sieve is vibrating sieve (3 ) is designed to be used in monolayers. The width (a) and length (L) of each rectangular mesh is 1.6 mm (width, a) x 16 mm (length, L). D is the diameter of the circular cross-section of the granular activated carbon cylinder to be held on the sieve. a = 0.75 h.

Preferably, a circular roller feeder or discharge circular roller G is provided at the bottom of each activated carbon supply chamber AC-c of the adsorption tower. In general, the adsorption tower has at least two activated carbon feed chambers (AC-c).

For the circular roller feeder or discharge circular roller G described herein, a circular roll feeder or discharge circular roller G in the prior art may be used as shown in FIGS. 10 and 11 . However, preferably, instead of the circular roller feeder or the discharging circular roller G, a star-wheel type activated carbon discharging device G as shown in FIG. 12 may be used. The new star-wheel type activated carbon discharging device (G) comprises a front baffle (AC-I) and a rear baffle (AC-II) in the lower part of the activated carbon supply chamber, and the front baffle (AC-I) and the rear baffle (AC-) II) and a star-wheel type activated carbon discharge roller (G) located below the discharge port formed by the two side plates at the bottom of the activated carbon supply chamber. The star-wheel type activated carbon discharging roller G comprises a circular roller G01 and a plurality of blades G02 distributed conformally or substantially conformally along the circumference of the circular roller. More specifically, the star-wheel type activated carbon discharge roller (G) is used below the discharge port formed by the front baffles (AC-I) and the rear baffles (AC-II) and two side plates at the bottom of the activated carbon supply chamber. . That is, the star-wheel type activated carbon discharging roller (G) is at the bottom of each material chamber at the bottom of the activated carbon bed, or at the bottom of the activated carbon supply chamber with the front baffle (AC-I) and the rear baffle (AC-II). It is mounted below the exhaust port formed by the side plates of the dog.

When viewed from the cross section of the star-wheel type activated carbon discharging roller (G), the star-wheel type activated carbon discharging roller exhibits a star-wheel configuration or shape.

Further, the new star-wheel type activated carbon discharging device may be referred to as a star-wheel type activated carbon discharging roller (G), or the two may be used interchangeably.

The star-wheel type activated carbon discharging device mainly includes a front baffle (AC-I) and a rear baffle (AC-II) and two side plates of the activated carbon discharging port, a blade (G02) and a circular roller (G01). The front baffle and the rear baffle are fixedly disposed, and the activated carbon exhaust passage, ie, the exhaust port, is between the front baffle and the rear baffle. The exhaust port includes a front baffle (AC-I), a rear baffle (AC-II), and two side plates. A circular roller is disposed at the lower end of the front baffle (AC-I) and at the lower end of the rear baffle (AC-II). The blades G02 are uniformly distributed and fixed on the circular rollers G01. The circular roller G01 is driven by a motor to rotate, and the direction of rotation is from the rear baffle (AC-II) to the front baffle (AC-I). The narrow angle or spacing between adjacent blades G02 should not be too large. The included angle θ between adjacent blades is generally less than 64°, for example 12° to 64°, preferably 15° to 60°, preferably 20° to 55°, more preferably 25° to 50°, even more preferably 30° to 45°. A gap or distance s is provided between the blade and the bottom of the rear baffle. s is generally from 0.5 mm to 5 mm, preferably from 0.7 mm to 3 mm, more preferably from 1 mm to 2 mm.

The radius of the outer circumference of the star-wheel type activated carbon discharging roller G (or the radius of rotation of the outer circumference of the blade on the circular roller) is r. r is equal to the radius of the cross section (circle) of the circular roller G01 plus the width of each blade G02.

In general, the radius of the cross section (circle) of the circular roller G01 is 30 mm to 120 mm, and the width of each blade G02 is 40 mm to 130 mm.

The distance between the center of the circular roller and the bottom of the front baffle is h. h is generally larger than r + (12 to 30)mm and smaller than r/sin58°, which can ensure that the activated carbon is discharged smoothly and that the activated carbon does not slide by itself when the circular roller is not moving.

In general, in the present disclosure, the cross section of the discharge port of the star-wheel type activated carbon discharging device is a square or rectangle, preferably a rectangle having a length greater than the width, that is, a rectangle having a length greater than the width.

Preferably, the evacuation vessel or bottom vessel 107 of the adsorption tower is provided with one or more evacuation rotary valves (F).

For the rotary valve F described herein, a rotary valve of the prior art may be used as shown in FIG. 10 . However, preferably, a new rotary valve F is used as shown in FIGS. 13 to 16 . The new rotary valve (F) has an upper supply port (F04), a valve core (F01), a blade (F02), a valve housing (F03), a lower outlet port (F05), and a buffer zone in the upper space of the internal cavity of the valve ( F06), and a material-smooth plate F07. The buffer zone F06 is adjacent to and in communication with the lower space of the supply port F04, and the length of the cross section of the buffer zone F06 in the horizontal direction is the length of the cross section of the supply port F04 in the horizontal direction. longer than The material-smooth plate is placed in the buffer zone F06, the upper end of the material-smooth plate F07 is fixed on top of the buffer zone F06, and the cross section of the material-smooth plate F07 is "V" in the horizontal direction “It has a shape.

Preferably, the cross section of the upper supply port F04 is rectangular, and the cross section of the buffer zone F06 is rectangular.

Preferably, the length of the cross-section of the buffer zone F06 is smaller than the length of the cross-section of the blade F02 in the horizontal direction.

Preferably, the material-smooth plate F07 is formed by splicing two single plates F0701, F0702, or the material-smooth plate F07 has two plate surfaces F0701, bent from one plate. F0702).

Preferably, the included angle between the two single plates F0701, F0702 or the two plate surfaces F0701, F0702 is 2α≦120°, preferably 2α≦90°. Accordingly, 2α≦60°, preferably 2α≦45°.

Preferably, the included angle between each single plate F0701, F0702 or each plate surface F0701, F0702 and the longitudinal direction of the buffer zone F06 is Φ≥30°, preferably Φ≥45°, more than Preferably, Φ≧is the friction angle of the activated carbon material.

Preferably, the bottom of each of the two single plates F0701, F0702 or the two plate surfaces F0701, F0702 is arc-shaped.

Preferably, the length of the centerline segment between the two single plates F0701, F0702 or the two plate surfaces F0701, F0702 is equal to or smaller than the width of the cross-section of the buffer zone F06 in the horizontal direction.

Obviously, α + Φ = 90°.

Generally, in the present disclosure, the cross section of the outlet port F05 of the new rotary valve F is a square or rectangle, preferably a rectangle having a length greater than the width, that is, a rectangle having a length greater than the width.

first embodiment

As shown in Figure 1, the desulfurization, denitrification and ammonia removal system includes an adsorption tower (1), a desorption tower (2), a distributor (3), a first activated carbon conveyor (4) and a second activated carbon conveyor (5) . The flue gas inlet A is provided on one side of the adsorption tower 1 . The flue gas outlet (B) is provided on another side of the adsorption tower (1). The adsorption chamber 103 and the ammonia removal chamber 104 are provided inside the adsorption tower 1 . The adsorption chamber 103 and the ammonia removal chamber 104 are disposed parallel to the adsorption tower 1 in a vertical direction. The adsorption chamber 103 is arranged on the side close to the flue gas inlet A. The ammonia removal chamber 104 is arranged on the side close to the flue gas outlet B. The first activated carbon conveyor 4 is connected to the discharge port of the adsorption tower 1 and the supply port of the distributor 3 . The second activated carbon conveyor 5 is connected to the discharge port of the desorption tower 2 and the supply port of the adsorption chamber 103 . The outlet port of the distributor 3 is connected to the feed port of the ammonia removal chamber 104 and the feed port of the desorption tower 2 . The thickness of the adsorption chamber 103 is three times the thickness of the ammonia removal chamber 104 .

The adsorption tower 1 has two activated carbon supply chambers AC-c as shown in FIG. 10 . A circular roller feeder G is provided at the outlet of each feed chamber AC-c. A rotary valve (F) is provided at the outlet of the discharge hopper or bottom vessel (H).

second embodiment

Similar to the first embodiment, except that a flue is provided downstream of the flue gas inlet A. The flue downstream of the flue gas inlet A is divided into two layers, the flue upper 101 and the flue lower 102, respectively. The flue top 101 is provided with an ammonia gas blowing device P. A porous plate 7 is provided between the adsorption chamber 103 and the ammonia removal chamber 104 . The adsorption chamber 103 is separated from the ammonia removal chamber 104 by a porous plate 7 . A vibrating sieve (8) is provided below the discharge port of the desorption tower (2). The vibrating sieve 8 is provided with a sieve according to Embodiment A. The front part of the second activated carbon conveyor 5 is connected to the discharge port of the vibrating sieve 8 . The thickness of the adsorption chamber 103 is 6 times the thickness of the ammonia removal chamber 104 .

third embodiment

It is similar to the second embodiment, except that the distributor 3 is provided with a sieve device, a large particle activated carbon outlet and a particulate activated carbon outlet. A large particle activated carbon outlet is disposed above the sieve device. A particulate activated carbon outlet is disposed below the sieve device. A large particle activated carbon outlet is connected to the supply port of the ammonia removal chamber 104 . The particulate activated carbon outlet is connected to the feed port of the desorption tower (2).

4th embodiment

2, the desulfurization, denitrification and ammonia removal system comprises an adsorption tower 1, a desorption tower 2, a first activated carbon conveyor 4 and a second activated carbon conveyor 5, and a storage vessel 6 include The flue gas inlet A is provided on one side of the adsorption tower 1 . The flue gas outlet (B) is provided on another side of the adsorption tower (1). The adsorption chamber 103 and the ammonia removal chamber 104 are provided inside the adsorption tower 1 . The adsorption chamber 103 and the ammonia removal chamber 104 are disposed parallel to the adsorption tower 1 in a vertical direction. The adsorption chamber 103 is arranged on the side close to the flue gas inlet A. The ammonia removal chamber 104 is arranged on the side close to the flue gas outlet B. The first activated carbon conveyor 4 is connected to the discharge port of the adsorption tower 1 and the supply port of the desorption tower 2 . The second activated carbon conveyor 5 is connected to the discharge port of the desorption tower 2 and the supply port of the adsorption chamber 103 . The tail end of the second activated carbon conveyor 5 is further connected to the supply port of the storage vessel 6 , and the discharge port of the storage vessel 6 is connected to the supply port of the ammonia removal chamber 104 .

This system further comprises an SO ₂ recovery system (R), a sulfur-rich gas transport pipeline (L1), and an SO ₂ recovery system tail gas transport pipeline (L2). One end of the sulfur-rich gas transport pipeline L1 is connected to a desorption tower 2 . The other end of the sulfur-rich gas delivery pipeline (L1) is connected to the gas inlet of the SO ₂ recovery system (R). One end of the SO ₂ recovery system tail gas delivery pipeline (L2) is connected to the gas outlet of the SO ₂ recovery system (R). The other end of the SO ₂ recovery system tail gas delivery pipeline L2 is connected to the gas inlet of the storage vessel 6 . The gas outlet of the storage vessel 6 is connected to the flue gas outlet B.

Preferably, a vibrating sieve 8 is provided below the discharge port of the desorption tower 2 . The vibrating sieve 8 is provided with a sieve according to Embodiment A.

5th embodiment

3, the desulfurization, denitrification and ammonia removal system comprises an adsorption tower 1, a desorption tower 2, a first activated carbon conveyor 4 and a second activated carbon conveyor 5, and a storage vessel 6 include The flue gas inlet A is provided on one side of the adsorption tower 1 . The flue gas outlet (B) is provided on another side of the adsorption tower (1). The adsorption chamber 103 and the ammonia removal chamber 104 are provided inside the adsorption tower 1 . The adsorption chamber 103 and the ammonia removal chamber 104 are disposed parallel to the adsorption tower 1 in a vertical direction. The adsorption chamber 103 is arranged on the side close to the flue gas inlet A. The ammonia removal chamber 104 is arranged on the side close to the flue gas outlet B. The first activated carbon conveyor 4 is connected to the discharge port of the adsorption tower 1 and the supply port of the desorption tower 2 . The second activated carbon conveyor 5 is connected to the discharge port of the desorption tower 2 and the supply port of the adsorption chamber 103 . The supply port of the storage vessel 6 is connected to a fresh activated carbon vessel. The discharge port of the storage vessel 6 is connected to the supply port of the ammonia removal chamber 104 .

This system further comprises an SO ₂ recovery system (R), a sulfur-rich gas transport pipeline (L1), and an SO ₂ recovery system tail gas transport pipeline (L2). One end of the sulfur-rich gas transport pipeline L1 is connected to a desorption tower 2 . The other end of the sulfur-rich gas delivery pipeline (L1) is connected to the gas inlet of the SO ₂ recovery system (R). One end of the SO ₂ recovery system tail gas delivery pipeline (L2) is connected to the gas outlet of the SO ₂ recovery system (R). The other end of the SO ₂ recovery system tail gas delivery pipeline L2 is connected to the gas inlet of the storage vessel 6 . The gas outlet of the storage vessel 6 is connected to the flue gas outlet B.

Preferably, a vibrating sieve 8 is provided below the discharge port of the desorption tower 2 . The vibrating sieve 8 is provided with a sieve according to Embodiment A.

6th embodiment

4, the desulfurization, denitrification and ammonia removal system comprises an adsorption tower 1, a desorption tower 2, a first activated carbon conveyor 4 and a second activated carbon conveyor 5, and a storage vessel 6 include The flue gas inlet A is provided on one side of the adsorption tower 1 . The flue gas outlet (B) is provided on another side of the adsorption tower (1). The adsorption chamber 103 and the ammonia removal chamber 104 are provided inside the adsorption tower 1 . The adsorption chamber 103 and the ammonia removal chamber 104 are disposed parallel to the adsorption tower 1 in a vertical direction. The adsorption chamber 103 is arranged on the side close to the flue gas inlet A. The ammonia removal chamber 104 is arranged on the side close to the flue gas outlet B. The first activated carbon conveyor 4 is connected to the discharge port of the adsorption tower 1 and the supply port of the desorption tower 2 . The second activated carbon conveyor 5 is connected to the discharge port of the desorption tower 2 and the supply port of the adsorption chamber 103 . The tail end of the second activated carbon conveyor 5 is further connected to the supply port of the storage vessel 6 , and the discharge port of the storage vessel 6 is connected to the supply port of the ammonia removal chamber 104 .

This system further comprises a raw flue gas branch (L3) and a raw flue gas recirculation transport pipeline (L4). One end of the raw flue gas branch L3 is connected to the front of the flue gas inlet A. The other end of the raw flue gas branch L3 is connected to the gas inlet of the storage vessel 6 . The gas outlet of the storage vessel 6 is connected to the rear of the flue gas inlet A via a raw flue gas recirculation transport pipeline L4.

Preferably, a vibrating sieve 8 is provided below the discharge port of the desorption tower 2 . The vibrating sieve 8 is provided with a sieve according to Embodiment A.

seventh embodiment

5, the desulfurization, denitrification and ammonia removal system comprises an adsorption tower 1, a desorption tower 2, a first activated carbon conveyor 4 and a second activated carbon conveyor 5, and a storage vessel 6 include The flue gas inlet A is provided on one side of the adsorption tower 1 . The flue gas outlet (B) is provided on another side of the adsorption tower (1). The adsorption chamber 103 and the ammonia removal chamber 104 are provided inside the adsorption tower 1 . The adsorption chamber 103 and the ammonia removal chamber 104 are disposed parallel to the adsorption tower 1 in a vertical direction. The adsorption chamber 103 is arranged on the side close to the flue gas inlet A. The ammonia removal chamber 104 is arranged on the side close to the flue gas outlet B. The first activated carbon conveyor 4 is connected to the discharge port of the adsorption tower 1 and the supply port of the desorption tower 2 . The second activated carbon conveyor 5 is connected to the discharge port of the desorption tower 2 and the supply port of the adsorption chamber 103 . The supply port of the storage vessel 6 is connected to a fresh activated carbon vessel. The discharge port of the storage vessel 6 is connected to the supply port of the ammonia removal chamber 104 .

This system further comprises a raw flue gas branch (L3) and a raw flue gas recirculation transport pipeline (L4). One end of the raw flue gas branch L3 is connected to the front of the flue gas inlet A. The other end of the raw flue gas branch L3 is connected to the gas inlet of the storage vessel 6 . The gas outlet of the storage vessel 6 is connected to the rear of the flue gas inlet A via a raw flue gas recirculation transport pipeline L4.

Preferably, a vibrating sieve 8 is provided below the discharge port of the desorption tower 2 . The vibrating sieve 8 is provided with a sieve according to Embodiment A.

eighth embodiment

Similar to the seventh embodiment, except that a flue is provided downstream of the flue gas inlet A. The flue downstream of the flue gas inlet A is divided into two layers, the flue upper 101 and the flue lower 102, respectively. The flue top 101 is provided with an ammonia gas blowing device P. An ammonia gas blowing device P is provided downstream of the flue gas (left as shown in FIG. 5 ) at the connection point of the raw flue gas branch L3 and the flue gas inlet A.

In the above-described embodiment, by using a vibrating sieve equipped with a special sieve instead of a conventional vibrating sieve under the outlet of the desorption tower 2, the bridging phenomenon of tablet-shaped activated carbon is eliminated, and a tablet having low abrasion resistance and compressive strength By sieving the shaped activated carbon to prevent debris and dust in the desulfurization and denitration device, the movement resistance of the activated carbon is reduced, the risk of high-temperature combustion of the activated carbon in the adsorption tower is reduced, the high-strength activated carbon is recycled in the device, and the filtration by the vibrating sieve decreases, and operating costs decrease.

9th embodiment

It is similar to the first embodiment, except that, instead of the discharge circular roller G, a new star-wheel type activated carbon discharging device G as shown in Fig. 12 is used. An exhaust port is provided at the bottom of the activated carbon supply chamber. The exhaust port includes a front baffle (AC-I), a rear baffle (AC-II), and two side plates (not shown).

The height of the main structure of the adsorption tower is 21 m (meters). The adsorption tower 1 has two activated carbon feed chambers. The thickness of the first chamber on the left is 180 mm. The thickness of the second chamber on the right is 900 mm.

The star-wheel type activated carbon discharging device includes a front baffle (AC-I) and a rear baffle (AC-II) in the lower part of the activated carbon supply chamber, and the front baffle (AC-I) and the rear baffle (AC-II) and the activated carbon supply and a star-wheel type activated carbon discharge roller (G) located below the discharge port formed by the two side plates at the bottom of the chamber. The star-wheel type activated carbon discharge roll G includes a circular roll G01 and twelve blades G02 distributed at an equal angle (θ = 30°) along the circumference of the circular roller.

When viewed from the cross section of the star-wheel type activated carbon discharging roller, the star-wheel type activated carbon discharging roller exhibits a star-wheel configuration.

The exhaust port includes a front baffle (AC-I), a rear baffle (AC-II), and two side plates. The circular rollers are disposed at the lower end of the front baffle (AC-I) and at the lower end of the rear baffle (AC-II). The blades G02 are uniformly distributed and fixed on the circular rollers G01. The circular roller G01 is driven by a motor to rotate, and the direction of rotation is from the rear baffle (AC-II) to the front baffle (AC-I). The included angle θ between the adjacent blades G02 is 30°. A gap or distance s is provided between the blade and the bottom of the rear baffle. The value of s is 2 mm.

The radius of the outer circumference of the star-wheel type activated carbon discharging roller G (or the radius of rotation of the outer circumference of the blade on the circular roller) is r. r is equal to the radius of the cross section (circle) of the circular roller G01 plus the width of each blade G02.

The radius of the cross section (circle) of the circular roller G01 is 60 mm, and the width of each blade G02 is 100 mm.

The distance between the center of the circular roller and the bottom of the front baffle is h. h is generally larger than r + (12 to 30)mm and smaller than r/sin58°, which can ensure that the activated carbon is discharged smoothly and that the activated carbon does not slide by itself when the circular roller is not moving.

tenth embodiment

It is similar to the second embodiment, except that, instead of the discharge circular roller G, a new star-wheel type activated carbon discharging device G as shown in Fig. 12 is used. An exhaust port is provided at the bottom of the activated carbon supply chamber. The exhaust port consists of a front baffle (AC-I), a rear baffle (AC-II), and two side plates (not shown).

The height of the main structure of the adsorption tower is 21 m (meters). The adsorption tower 1 has two activated carbon feed chambers. The thickness of the first chamber on the left is 160 mm. The thickness of the second chamber on the right is 1000 mm.

The star-wheel type activated carbon discharging device includes a front baffle (AC-I) and a rear baffle (AC-II) in the lower part of the activated carbon supply chamber, and the front baffle (AC-I) and the rear baffle (AC-II) and the activated carbon supply and a star-wheel type activated carbon discharge roller (G) located below the discharge port formed by the two side plates at the bottom of the chamber. The star-wheel type activated carbon discharge roll G comprises a circular roll G01 and eight blades G02 distributed at an equal angle (θ = 45°) along the circumference of the circular roller.

When viewed from the cross section of the star-wheel type activated carbon discharging roller, the star-wheel type activated carbon discharging roller exhibits a star-wheel configuration.

The exhaust port includes a front baffle (AC-I), a rear baffle (AC-II), and two side plates. A circular roller is disposed at the bottom of the front baffle (AC-I) and the rear baffle (AC-II). The blades G02 are uniformly distributed and fixed on the circular rollers G01. The circular roller G01 is driven by a motor to rotate, and the direction of rotation is from the rear baffle (AC-II) to the front baffle (AC-I). The included angle θ between the adjacent blades G02 is 45°. A gap or distance s is provided between the blade and the bottom of the rear baffle. The value of s is 1 mm.

The radius of the outer circumference of the star-wheel type activated carbon discharging roller G is r. r is equal to the radius of the cross section (circle) of the circular roller G01 plus the width of each blade G02.

The radius of the cross section (circle) of the circular roller G01 is 90 mm, and the width of each blade G02 is 70 mm.

The distance between the center of the circular roller and the bottom of the front baffle is h. h is generally larger than r + (12 to 30)mm and smaller than r/sin58°, which can ensure that the activated carbon is discharged smoothly and that the activated carbon does not slide by itself when the circular roller is not moving.

11th embodiment

It is similar to the second embodiment, except that instead of the conventional discharge rotary valve F, a new type of discharge rotary valve F as shown in Figs. 13 to 16 is used.

The new rotary valve (F) has an upper supply port (F04), a valve core (F01), a blade (F02), a valve housing (F03), a lower outlet port (F05), and a buffer zone in the upper space of the internal cavity of the valve ( F06), and a material-smooth plate F07. The buffer zone F06 is adjacent to and in communication with the lower space of the supply port F04, and the length of the cross section of the buffer zone F06 in the horizontal direction is the length of the cross section of the supply port F04 in the horizontal direction. longer than The material-smooth plate is placed in the buffer zone F06, the upper end of the material-smooth plate F07 is fixed on top of the buffer zone F06, and the cross section of the material-smooth plate F07 is "V" in the horizontal direction “It has a shape.

The cross section of the upper supply port F04 is rectangular, and the cross section of the buffer zone F06 is also rectangular.

The length of the cross-section of the buffer zone F06 is smaller than the length of the cross-section of the blade F02 in the horizontal direction.

The material-smooth plate F07 is formed by splicing two single plates F0701 and F0702.

The included angle 2α between the two single plates F0701 and F0702 is 90°.

Preferably, the included angle Φ between each single plate F0701 , F0702 and the longitudinal direction of the buffer zone F06 or between each plate surface F0701 , F0702 and the longitudinal direction of the buffer zone F06 is 30 is °. Φ must exceed the friction angle of the activated carbon material.

The bottom of each of the two single plates F0701 and F0702 has an arc shape.

Preferably, the length of the centerline segment between the two single plates F0701, F0702 or the two plate surfaces F0701, F0702 is slightly smaller than the width of the cross-section of the buffer zone F06 in the horizontal direction.

α + Φ = 90°.

The radius of rotation of the outer circumference of the blade on the circular roller is r. r is equal to the radius of the cross-section (circle) of the valve core F01 plus the width of each blade F02.

The radius of the cross section (circle) of the valve core F01 is 30 mm, and the width of each blade F02 is 100 mm. Therefore, r is 130 mm.

The length of the blade F02 is 380 mm.

12th embodiment

It is similar to the tenth embodiment, except that instead of the conventional discharge rotary valve F, a new type of discharge rotary valve F as shown in Figs. 13 to 16 is used.

The new rotary valve (F) has an upper supply port (F04), a valve core (F01), a blade (F02), a valve housing (F03), a lower outlet port (F05), and a buffer zone in the upper space of the internal cavity of the valve ( F06), and a material-smooth plate F07. The buffer zone F06 is adjacent to and in communication with the lower space of the supply port F04, and the length of the cross section of the buffer zone F06 in the horizontal direction is the length of the cross section of the supply port F04 in the horizontal direction. longer than The material-smooth plate is placed in the buffer zone F06, the upper end of the material-smooth plate F07 is fixed on top of the buffer zone F06, and the cross section of the material-smooth plate F07 is "V" in the horizontal direction “It has a shape.

The cross section of the upper supply port F04 is rectangular, and the cross section of the buffer zone F06 is also rectangular.

The length of the cross-section of the buffer zone F06 is smaller than the length of the cross-section of the blade F02 in the horizontal direction.

The material-smooth plate F07 is formed by splicing two single plates F0701 and F0702.

The included angle 2α between the two single plates F0701 and F0702 is 90°.

Preferably, the included angle Φ between each single plate F0701 , F0702 and the longitudinal direction of the buffer zone F06 or between each plate surface F0701 , F0702 and the longitudinal direction of the buffer zone F06 is 30 is °. Φ must exceed the friction angle of the activated carbon material.

The bottom of each of the two single plates F0701 and F0702 has an arc shape.

Preferably, the length of the centerline segment between the two single plates F0701, F0702 or the two plate surfaces F0701, F0702 is slightly smaller than the width of the cross-section of the buffer zone F06 in the horizontal direction.

α + Φ = 90°.

The radius of rotation of the outer circumference of the blade on the circular roller is r. r is equal to the radius of the cross-section (circle) of the valve core F01 plus the width of each blade F02.

The radius of the cross section (circle) of the valve core F01 is 30 mm, and the width of each blade F02 is 100 mm. Therefore, r is 130 mm.

The length of the blade F02 is 380 mm.

Reference signs are as follows:
1: adsorption tower
101: year upper
102: lower year
103: adsorption chamber
104: ammonia removal chamber
2: Desorption tower
3: Divider
4: first activated carbon conveyor
5: 2nd activated carbon conveyor
6: storage container
7: Porous plate
8: vibrating sieve
A: flue gas inlet
B: flue gas outlet
R: SO ₂ recovery system
P: ammonia gas blower
L1： Sulfur-rich gas transport pipeline
L2: SO ₂ recovery system tail gas transport pipeline
L3: Untreated flue gas branch
L4: Raw flue gas recovery transport pipeline
AC-c: activated carbon supply chamber
H: discharge hopper or lower container
AC: activated carbon
AC-1: Activated carbon lump (or aggregate)
F: Rotary valve
G: Round roller feeder or star-wheel type activated carbon discharge device or star-wheel type activated carbon discharge roller
G01: Circular roller
G02: Blade
AC-I: front baffle
AC-II: rear baffle
h: the distance between the central axis of the circular roller (G01) and the lower end of the front baffle (AC-I)
S: Distance (gap) between the blade and the bottom of the rear baffle
θ: the angle between adjacent blades G02 on the circular roller G01
r: the distance between the outer edge of the blade and the central axis of the circular roller G01 (that is, the radius of the blade with respect to the center of the circular roller G01, in short, the radius)
F: supply rotary valve
F01: valve core
F02: Blade
F03: valve housing
F04: Upper supply port
F05: Lower exhaust port
F06: Buffer band located in the upper space of the internal cavity of the valve
F07: Material-Smooth Plate
F0701 or F0702: Two single plates or two plate surfaces of material-smooth plate (F07)
α: half (1/2) of the angle between two single plates F0701, F0702 or two plate surfaces F0701, F0702
Φ: the angle between each single plate (F0701 or F0702) or each plate surface (F0701 or F0702) and the longitudinal direction of the buffer zone F06
L1: Length of the cross-section of the supply port (F04) in the horizontal direction
L2: the length of the cross-section of the material-smooth plate (F07) in the horizontal direction

Claims (18)

A desulfurization, denitrification and ammonia removal system comprising an adsorption tower (1), a desorption tower (2), a distributor (3), a first activated carbon conveyor (4) and a second activated carbon conveyor (5),
A flue gas inlet (A) is provided on one side of the adsorption tower (1), and a flue gas outlet (B) is provided on the other side of the adsorption tower (1), and adsorption inside the adsorption tower (1) A chamber 103 and an ammonia removal chamber 104 are provided, wherein the adsorption chamber 103 and the ammonia removal chamber 104 are disposed perpendicularly and parallel to the adsorption tower 1 , the adsorption chamber 103 comprising: is disposed on a side close to the flue gas inlet (A), and the ammonia removal chamber (104) is disposed on a side close to the flue gas outlet (B); The first activated carbon conveyor 4 is connected to the discharge port of the adsorption tower 1 and the supply port of the distributor 3, and the second activated carbon conveyor 5 is connected to the discharge port of the desorption tower 2 and the connected to the supply port of the adsorption chamber (103), the outlet port of the distributor (3) being connected to the supply port of the ammonia removal chamber (104) and the supply port of the desorption tower (2);
Desulfurization, denitrification and ammonia removal systems. A desulfurization, denitrification and ammonia removal system comprising an adsorption tower (1), a desorption tower (2), a first activated carbon conveyor (4) and a second activated carbon conveyor (5), and a storage vessel (6), the system comprising:
A flue gas inlet (A) is provided on one side of the adsorption tower (1), and a flue gas outlet (B) is provided on another side of the adsorption tower (1), an adsorption chamber (103) and an ammonia removal chamber (104) is provided inside the adsorption tower 1 , the adsorption chamber 103 and the ammonia removal chamber 104 are disposed perpendicularly and parallel to the adsorption tower 1 , and the adsorption chamber 103 is the flue gas disposed on the side close to the inlet (A), and wherein the ammonia removal chamber (104) is disposed on the side close to the flue gas outlet (B); The first activated carbon conveyor 4 is connected to the discharge port of the adsorption tower 1 and the supply port of the desorption tower 2, and the second activated carbon conveyor 5 is the discharge port of the desorption tower 2 and connected to the supply port of the adsorption chamber (103), alternatively the tail end of the second activated carbon conveyor (5) is further connected to the supply port of the storage vessel (6), an exhaust port is connected to the supply port of the ammonia removal chamber (104);
The system further comprises an SO ₂ recovery system (R), a sulfur-rich gas transport pipeline (L1), and an SO ₂ recovery system tail gas transport pipeline (L2), wherein the sulfur-rich gas transport pipeline One end of (L1) is connected to the desorption tower (2), and the other end of the sulfur-rich gas transport pipeline (L1) is connected to the gas inlet of the SO ₂ recovery system (R), the SO One end of the ₂ recovery system tail gas conveying pipeline L2 is connected to the gas outlet of the SO ₂ recovery system R, and the other end of the SO ₂ recovery system tail gas conveying pipeline L2 is connected to the storage connected to the gas inlet of the vessel (6), the gas outlet of the storage vessel (6) being connected to the flue gas outlet (B),
Desulfurization, denitrification and ammonia removal systems. A desulfurization, denitrification and ammonia removal system comprising an adsorption tower (1), a desorption tower (2), a first activated carbon conveyor (4) and a second activated carbon conveyor (5), and a storage vessel (6), the system comprising:
A flue gas inlet (A) is provided on one side of the adsorption tower (1), and a flue gas outlet (B) is provided on another side of the adsorption tower (1), an adsorption chamber (103) and an ammonia removal chamber (104) is provided inside the adsorption tower 1 , the adsorption chamber 103 and the ammonia removal chamber 104 are disposed perpendicularly and parallel to the adsorption tower 1 , and the adsorption chamber 103 is the flue gas disposed on the side close to the inlet (A), and wherein the ammonia removal chamber (104) is disposed on the side close to the flue gas outlet (B); The first activated carbon conveyor 4 is connected to the discharge port of the adsorption tower 1 and the supply port of the desorption tower 2, and the second activated carbon conveyor 5 is the discharge port of the desorption tower 2 and connected to the supply port of the adsorption chamber (103), alternatively the tail end of the second activated carbon conveyor (5) is further connected to the supply port of the storage vessel (6), the storage vessel (6) an outlet port of the Ammonia removal chamber (104) is connected to the supply port;
The system further comprises a raw flue gas branch (L3) and a raw flue gas recirculation conveying pipeline (L4), one end of the raw flue gas branch (L3) having the flue gas inlet (A) ), the other end of the raw flue gas branch L3 is connected to the gas inlet of the storage vessel 6, and the gas outlet of the storage vessel 6 is connected to the raw flue gas recirculation conveying pipe connected to the rear of the flue gas inlet (A) via a line (L4),
Desulfurization, denitrification and ammonia removal systems. The method of claim 1,
A flue is provided downstream of the flue gas inlet (A), the flue downstream of the flue gas inlet (A) is divided into two layers, namely flue upper 101 and flue lower 102, the flue A desulfurization, denitrification and ammonia removal system, wherein an ammonia gas blowing device (P) is provided in the upper portion (101). 4. The method of claim 3,
A flue is provided downstream of the flue gas inlet (A), the flue downstream of the flue gas inlet (A) is divided into two layers, namely flue upper 101 and flue lower 102, the flue An ammonia gas blowing device P is provided in the upper part 101; and the ammonia gas blowing device (P) is provided downstream of the flue at the connecting position of the raw flue gas branch (L3) and the flue gas inlet (A). 6. The method according to any one of claims 1 to 5,
A porous plate (7) is provided between the adsorption chamber (103) and the ammonia removal chamber (104), wherein the adsorption chamber (103) is separated from the ammonia removal chamber (104) by the porous plate (7) , desulfurization, denitrification and ammonia removal systems. 6. The method according to any one of claims 1 to 5,
Desulfurization, wherein a vibration sieve (8) is provided below the discharge port of the desorption tower (2), and the front part of the second activated carbon conveyor (5) is connected to the discharge port of the vibrating sieve (8); Denitrification and ammonia removal system. 6. The method according to any one of claims 1 to 5,
The thickness of the adsorption chamber (103) is 1 to 10 times the thickness of the ammonia removal chamber (104), desulfurization, denitrification and ammonia removal system. The method of claim 1,
The distributor (3) is provided with a sieve device, a large particle activated carbon outlet and a particulate activated carbon outlet, the large particle activated carbon outlet being disposed above the sieve device, the particulate activated carbon outlet being disposed below the sieving device, and , the large particle activated carbon outlet is connected to the supply port of the ammonia removal chamber (104), and the particulate activated carbon outlet is connected to the supply port of the desorption tower (2);
The sieve device is provided with a sieve having a rectangular mesh, wherein the length L of each rectangular mesh is 3D or more, and the width a of each rectangular mesh is 0.65h to 0.95h, where D is the length of the activated carbon cylinder held on the sieve. Desulfurization, denitrification and ammonia removal system, wherein h is the diameter of the circular cross section and h is the minimum length of the granular activated carbon cylinder held on the sieve. 4. The method of claim 2 or 3,
A vibrating sieve equipped with a sieve having a rectangular mesh is provided below the discharge port at the bottom of the desorption tower 2 or is provided downstream of the desorption tower 2, the length L of each rectangular mesh is 3D or more, the width a of each rectangular mesh is 0.65 h to 0.95 h, where D is the diameter of the circular cross-section of the activated carbon cylinder held on the sieve, and h is the minimum length of the granular activated carbon cylinder held on the sieve, Denitrification and ammonia removal system. 10. The method according to any one of claims 1 to 5 and 9,
The adsorption tower (1) has at least two activated carbon supply chambers (AC-c), at the bottom of each activated carbon supply chamber (AC-c) or a front baffle (AC-I) and a rear baffle (AC-II) and A star-wheel type activated carbon discharge roller (G) is mounted under the discharge port formed by two side plates in the lower part of the activated carbon supply chamber, and the star-wheel type activated carbon discharge roller (G) is a circular roller (G01) and a plurality of blades (G02) distributed equiangularly along the circumference of the circular roller. 12. The method of claim 11,
The circular roller G01 is disposed at the lower end of the front baffle AC-I and the rear baffle AC-II, and is a narrow angle between adjacent blades G02 distributed on the circumference of the circular roller G01. included angle) (θ) is 12° to 64°, desulfurization, denitrification and ammonia removal system. 13. The method of claim 12,
the distance s provided between the blade G02 and the lower end of the rear baffle is between 0.5 mm and 5 mm;
The radius of the cross section (circle) of the circular roller G01 is 30 mm to 120 mm, and the width of the blade G02 is 40 mm to 130 mm;
the distance (h) between the center of the circular roller and the lower end of the front baffle is greater than r + (12 to 30) mm and less than r/sin58°;
Desulfurization, denitrification and ammonia removal systems. 10. The method according to any one of claims 1 to 5 and 9,
At least one discharge rotary valve (F) is provided in the discharge vessel or bottom vessel (H) of the adsorption tower, said rotary valve (F) comprising an upper supply port (F04), a valve core (F01), a blade (F02), a valve a housing F03, a lower outlet port F05, a buffer zone F06 in the upper space of the internal cavity of the valve, and a material-smoothing plate F07; The buffer zone F06 is adjacent to and in communication with the lower space of the supply port F04, and the length of the cross section in the horizontal direction of the buffer zone F06 is the horizontal direction of the supply port F04. longer than the length of the cross-section into the furnace; The material-smooth plate is disposed in the buffer zone F06, the upper end of the material-smooth plate F07 is fixed to the upper part of the buffer zone F06, and the cross section of the material-smooth plate F07 is Desulfurization, denitrification and ammonia removal system, having a "V" shape in the horizontal direction. 15. The method of claim 14,
the cross section of the upper supply port F04 is rectangular, and the cross section of the buffer zone F06 is rectangular;
the length of the cross-section of the buffer zone F06 is smaller than the length of the cross-section of the blade F02 in the horizontal direction;
Desulfurization, denitrification and ammonia removal systems. 15. The method of claim 14,
The material-smooth plate F07 is formed by splicing two single plates F0701, F0702, or the material-smooth plate F07 is formed by bending two plate surfaces F0701 from one plate. , F0702), and the included angle (2α) between the two single plates (F0701, F0702) or the two plate surfaces (F0701, F0702) is ≤120°, that is, α≤60°, desulfurization, denitrification and ammonia removal system . 15. The method of claim 14,
The narrow angle Φ between each single plate F0701, F0702 and the longitudinal direction of the buffer zone F06, or the narrow angle between each plate surface F0701, F0702 and the longitudinal direction of the buffer zone F06, Φ) is ≧30°;
The bottom of each of the two single plates (F0701, F0702) or the two plate surfaces (F0701, F0702) is an arc shape,
Desulfurization, denitrification and ammonia removal systems. 3. The method of claim 2,
A flue is provided downstream of the flue gas inlet (A), the flue downstream of the flue gas inlet (A) is divided into two layers, namely flue upper 101 and flue lower 102, the flue A desulfurization, denitrification and ammonia removal system, wherein an ammonia gas blowing device (P) is provided in the upper portion (101).

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