CN210934467U - Internal circulating fluidized bed coupled heat exchanger integrated desulfurization and denitrification device - Google Patents

Abstract

The utility model discloses an integrated desulfurization and denitration device coupled with an internal circulating fluidized bed coupled with a heat exchanger, comprising: a heat exchanger for heat exchange between flue gas and a reducing agent; an internal circulating fluidized bed reactor equipped with a catalyst The top is provided with a flue gas outlet, and the interior is divided into a cyclically connected adsorption zone and a reduction zone by a vertically arranged partition. The side wall opening of the adsorption zone near the bottom is connected to the flue gas outlet of the heat exchanger, so The opening of the side wall near the bottom of the reduction zone is connected to the reducing agent outlet of the heat exchanger, and perforated plates for uniform gas distribution are provided at the inlet of the flue gas in the adsorption zone and at the inlet of the reducing agent in the reduction zone. Oxygen sensor, temperature sensor and pressure sensor are arranged on the side wall of the reduction zone. The utility model can realize the synchronous desulfurization and denitration efficiency of more than 70%, and solves the problem of excessive oxygen inhibiting the catalytic reduction process and the poisoning of the catalyst by the reduction product sulfur element.

Description

Internal circulating fluidized bed coupled heat exchanger integrated desulfurization and denitrification device

technical field

The utility model relates to the technical field of flue gas treatment, in particular to an integrated desulfurization and denitration device with an inner circulating fluidized bed coupled with a heat exchanger.

Background technique

Compound air pollution is a key issue of current scientific research at home and abroad, and it is also a hot social issue affecting the production and life of the public in my country. Sulfur oxides (SO _x ) and nitrogen oxides (NO _x ) are important precursors of secondary particulate matter and ozone in the atmosphere, mainly from stationary emission sources such as thermal power plants, heating boilers, chemical plants, automobiles, airplanes, etc. Mobile emission sources.

The existing flue gas (or tail gas) desulfurization and denitrification mostly adopts a hierarchical treatment method, that is, desulfurization and denitrification are respectively performed in different treatment devices. Desulfurization methods include dry desulfurization and wet desulfurization. Dry desulfurization technology is widely used due to its small footprint and high efficiency. Selective catalytic reduction (SCR) is a widely used denitration technology, which utilizes a reducing agent (mainly NH ₃ ) under the action of a catalyst (V ₂ O ₅ -WO ₃ /TiO ₂ ) to reduce NO _x to nitrogen.

Although the technology of separate denitrification and desulfurization by grading is relatively mature at this stage, the method of grading treatment has disadvantages such as high investment and operating costs, large occupation area and complex flue gas (or tail gas) treatment system. Therefore, the development of integrated desulfurization and denitrification technology has become a current hotspot.

The integrated desulfurization and denitrification technologies that have been studied so far are mainly wet simultaneous desulfurization and denitrification processes, such as chloric acid oxidation. The wet simultaneous desulfurization and denitrification process has the problems of secondary treatment and pollution of the absorption liquid, at the same time, the equipment is easy to corrode and the energy consumption is high. Therefore, it is necessary to develop a new dry integrated desulfurization and denitrification technology.

In the 1960s, Chevron Corporation of the United States took the lead in carrying out the research of dry integrated desulfurization and denitrification. The study found that CO can simultaneously catalytically reduce SO ₂ and NO on Cu/Al ₂ O ₃ catalyst in a fixed bed reactor. _x is elemental sulfur and N ₂ . However, the problem of inhibiting the catalytic reduction process due to excess oxygen (greater than 4 vol%) in the flue gas (or tail gas) cannot be solved, which limits the industrial application of this technology.

Utility model content

Aiming at the deficiencies in the art and the problem of excessive oxygen inhibiting the catalytic reduction process, the utility model provides an integrated desulfurization and denitration device with an inner circulating fluidized bed coupled with a heat exchanger, which can synchronous catalytic reduction with high efficiency and energy saving. SO ₂ and NO _x .

An integrated desulfurization and denitrification device with an internal circulating fluidized bed coupled heat exchanger, comprising:

heat exchanger for heat exchange of flue gas and reducing agent;

The internal circulating fluidized bed reactor equipped with catalyst has a flue gas outlet at the top, and the interior is divided into an adsorption zone and a reduction zone that are circulated and communicated by a vertically arranged partition. The flue gas outlet of the heat exchanger is connected, the side wall opening near the bottom of the reduction zone is connected to the reductant outlet of the heat exchanger, and the flue gas inlet of the adsorption zone and the reductant inlet of the reduction zone are equipped with uniform In the porous plate for gas distribution, oxygen sensors, temperature sensors and pressure sensors are provided on the side walls of the adsorption zone and the reduction zone.

The utility model adopts the inner circulating fluidized bed to replace the traditional fixed bed as the catalytic reactor, adopts the built-in baffle to separate the inner circulating fluidized bed into two connected reaction zones (adsorption zone and reduction zone), and separates the flue gas and the reduction zone. The catalyst is injected into the adsorption zone and the reduction zone respectively, and the circulation rate of the catalyst and the oxygen concentration distribution in the adsorption zone and the reduction zone can be controlled by adjusting the flow rate of the flue gas and the reducing agent. In the adsorption zone of high oxygen concentration, the catalyst can simultaneously adsorb SO ₂ and NO _x ; in the reduction zone of low oxygen concentration, the reducing agent can rapidly and simultaneously reduce the adsorbed SO ₂ and NO _x to sulfur element and N ₂ , wherein the product N ₂ and the treated flue gas are discharged through the exhaust outlet at the top of the internal circulating fluidized bed, and the product sulfur element is liquid in the internal circulating fluidized bed reactor, and is discharged in time through the porous plate and flows into the bottom of the internal circulating fluidized bed for collection. The utility model solves the problem of inhibition of synchronous catalytic reduction desulfurization and denitration reaction by high oxygen concentration and liquid sulfur element, and realizes the purpose of synchronously integrated desulfurization and denitration.

The higher the temperature, the worse the adsorption capacity of the gas on the catalyst surface. The utility model adopts a heat exchanger to conduct heat exchange between the flue gas and the reducing agent, reduces the temperature of the flue gas entering the adsorption zone, and increases the temperature of the reducing agent entering the reducing zone, so as to improve the adsorption and reduction effects of SO ₂ and NO _X respectively, and achieve The purpose of high efficiency and energy saving.

Preferably, the inner circulating fluidized bed reactor is cylindrical. Further preferably, the height-diameter ratio of the inner circulating fluidized bed reactor is 8-12:1.

In order to achieve better adsorption, reduction balance and distribution control of oxygen content, preferably, the volume ratio of the adsorption zone to the reduction zone is 3-5:1.

Preferably, a catalyst collection chamber is provided in the middle of the inner bottom of the inner circulating fluidized bed reactor, below the adsorption zone and the reduction zone, a catalyst collection valve is provided on the top surface of the catalyst collection chamber, and a catalyst discharge valve is provided on the bottom surface. The catalyst collection chamber is used to collect and discharge poisoned and deactivated catalysts, so as to facilitate the replacement of new catalysts.

By adjusting the size of the gap left at the top and bottom of the separator, the distribution of oxygen content in the adsorption zone and the reduction zone can be further controlled. The ratio of the distance to the height of the inner circulating fluidized bed reactor is 3 to 6:100;

The ratio of the distance between the bottom end of the partition plate and the top surface of the catalyst collection chamber to the height of the inner circulating fluidized bed reactor is 3-6:100.

The sulfur element of the SO ₂ reduction product is in a liquid state under the reduction reaction conditions, and the excessive accumulation of the liquid sulfur element will lead to poisoning and rapid deactivation of the catalyst. Preferably, the bottom end of the porous plate is fixedly connected to the side wall of the catalyst collection chamber, and the top It is fixedly connected with the side wall of the inner circulating fluidized bed reactor, and the perforated plate, the side wall of the catalyst collection chamber, the side wall and the bottom surface of the inner circulating fluidized bed reactor enclose an elemental sulfur collection chamber;

The elemental sulfur collection chamber is provided with an elemental sulfur discharge valve on the bottom surface, which facilitates the timely discharge of elemental sulfur.

Further preferably, the perforated plate is inclined, the bottom end is fixedly connected with the top end of the side wall of the catalyst collection chamber, and the top end is fixedly connected with the side wall above the inlet of the flue gas or reducing agent of the inner circulating fluidized bed reactor, which avoids the need for a The accumulation of liquid sulfur in the adsorption zone or reduction zone is beneficial to the discharge of sulfur.

Preferably, the ratio of the mass of the catalyst to the volume of the inner circulating fluidized bed reactor is 20-40 kg:1 m ³ .

Preferably, a catalyst adding valve is provided on the top surface of the adsorption zone, which is beneficial for the fresh catalyst added to directly enter the adsorption zone for adsorption.

The process flow of the internal circulating fluidized bed coupled heat exchanger integrated desulfurization and denitrification device during operation includes the steps:

(1) The high temperature flue gas and reducing agent containing SO ₂ and NO _x are both 200-300 °C after heat exchange in the heat exchanger, and then enter the adsorption zone and the reduction zone respectively, and the flue gas passes through the catalyst in the adsorption zone. Then, it is discharged through the flue gas outlet, and at the same time, SO ₂ and NO _x are in contact with the catalyst in the adsorption zone and are adsorbed;

(2) The catalyst adsorbed with SO ₂ and NO _x in the adsorption zone crosses the separator and enters the reduction zone under the driving of the airflow, and the SO ₂ and NO _x adsorbed on the surface of the catalyst are reduced by the reducing agent entering the reduction zone into liquid elemental sulfur and N ₂ , elemental sulfur enters the elemental sulfur collection chamber through the porous plate, and N ₂ flows back to the adsorption zone through the gap under the separator with the airflow to mix with the incoming flue gas;

(3) Driven by the airflow, the catalyst that has undergone the reduction reaction, the surface SO ₂ and NO _x desorption is completely desorbed, and flows back to the adsorption zone through the gap under the separator to enter the next round of SO ₂ and NO _x adsorption;

(4) Circulation steps (1) to (3), realize the integrated desulfurization and denitrification of the inner circulating fluidized bed coupled with the heat exchanger.

Preferably, the ratio of flue gas flow to reducing agent flow is 1 to 2:1;

The residence time of flue gas in the adsorption zone is 5-20s, the concentration of SO ₂ is 400-1000ppm, the concentration of _NOx is 300-500ppm, and the concentration of oxygen is 5-10vol%;

The residence time of the reducing agent in the reduction zone is 3-6 s, the concentration of the reducing agent is 1-3 vol%, and the oxygen concentration is 1-4 vol%.

By adjusting the flow rate of flue gas and reducing agent to control the circulation rate of the catalyst, as well as the oxygen concentration in the adsorption zone and the reduction zone, the gas _- solid adsorption of SO2 and _NOx with the catalyst is enhanced in the adsorption zone with high oxygen content (5-10 vol%) , in the reduction zone with low oxygen content (1-4 vol%), the efficiency of the reducing agent for catalytic reduction of SO ₂ and NO _x is improved.

Preferably, the reducing agent is H ₂ , CO or hydrocarbons. Alkaline reducing agents such as _NH3 are easy to react with SO2 to form _sulfate or sulfite, resulting in the inability of SO2 to be reduced.

The catalyst should have excellent adsorption capacity for SO ₂ and NO _x , and high-efficiency catalytic reduction performance for SO ₂ and NO _x . Preferably, the catalyst is a supported transition metal oxide and/or a rare earth-transition metal composite oxide.

Compared with the prior art, the utility model has the following main advantages: the utility model can realize the synchronous desulfurization and denitration efficiency of over 70%, the heat exchanger can reduce the energy consumption by 15% to 20%, and solve the problem of excessive oxygen on the catalytic reduction process. The problem of inhibition, and the poisoning of the catalyst by the reduction product sulfur element.

Description of drawings

1 is a schematic structural diagram of an integrated desulfurization and denitrification device with an internal circulating fluidized bed coupled heat exchanger according to an embodiment;

In the figure: 1- the reductant inlet of the heat exchanger, 2- the flue gas inlet of the heat exchanger, 3- the reductant outlet of the heat exchanger, 4- the flue gas outlet of the heat exchanger, 5- the flue gas inlet of the adsorption zone , 6- reduction zone reducing agent inlet, 7- internal circulating fluidized bed reactor flue gas outlet, 8- circulating flow direction of granular catalyst, 9- heat exchanger, 10- internal circulating fluidized bed reactor, 11- Elemental sulfur collection chamber, 12-catalyst collection chamber, 13-catalyst collection chamber discharge valve, 14-catalyst collection chamber collection valve, 15-elemental sulfur discharge valve, 16-porous plate, 17-oxygen sensor, 18-temperature sensor, 19 - Pressure sensor, 20 - Separator, 21 - Catalyst addition valve, 22 - Adsorption zone, 23 - Reduction zone.

Detailed ways

The present utility model will be further described below with reference to the accompanying drawings and specific embodiments. It should be understood that these embodiments are only used to illustrate the present invention and not to limit the scope of the present invention. The operation method without specifying the specific conditions in the following examples is usually in accordance with the conventional conditions, or in accordance with the conditions suggested by the manufacturer.

The integrated desulfurization and denitrification device with an internal circulating fluidized bed coupled with a heat exchanger in this embodiment includes: a heat exchanger 9 and an internal circulating fluidized bed reactor 10 . The internal circulating fluidized bed reactor 10 is cylindrical, and the height-diameter ratio is 10:1.

The interior of the internal circulating fluidized bed reactor 10 is divided into an adsorption zone 22 and a reduction zone 23 which are circulated and communicated by a vertically arranged partition 20. The volume ratio of the adsorption zone 22 to the reduction zone 23 is 3 to 5:1, and the adsorption zone 22 Granular catalysts are installed in the reduction zone 23, and the ratio of the mass of the catalyst to the effective volume of the inner circulating fluidized bed reactor 10 is 30kg: ^1m3 . The catalyst is a supported transition metal oxide or rare earth-transition metal composite oxide

A catalyst collection chamber 12 is provided in the middle of the inner circulating fluidized bed reactor 10 below the adsorption zone 22 and the reduction zone 23 . The ratio of the distance H between the top of the partition plate 20 and the top surface of the internal circulating fluidized bed reactor 10 to the height of the internal circulating fluidized bed reactor 10 is 1:20. The ratio between the distance h and the height of the inner circulating fluidized bed reactor 10 is 1:20. Both sides of the partition plate 20 are fixedly connected with the side walls of the internal circulating fluidized bed reactor 10, the connection is completely sealed, and the adsorption zone 22 and the reduction zone 23 only pass between the top of the partition plate 20 and the top surface of the internal circulating fluidized bed reactor 10. The gap between the two, and the gap between the top of the separator 20 and the top surface of the catalyst collection chamber 12 communicates and circulates.

The two side walls of the catalyst collection chamber 12 parallel to the partition plate 20 are also fixedly connected to the side walls of the inner circulating fluidized bed reactor 10, the connection is completely sealed, and the length perpendicular to the direction of the partition plate 20 is smaller than that of the inner circulating fluidized bed reactor. 10 width.

The side wall of the internal circulating fluidized bed reactor 10 on the side of the adsorption zone 22 is provided with an adsorption zone flue gas inlet 5 near the bottom, and an oxygen sensor 17, a temperature sensor 18 and a pressure sensor 19 are arranged above the adsorption zone flue gas inlet 5. . A catalyst addition valve 21 and a flue gas outlet 7 are provided on the top surface of the inner circulating fluidized bed reactor 10 on one side of the adsorption zone 22 .

The side wall of the inner circulating fluidized bed reactor 10 on the side of the reduction zone 23 is provided with a reduction zone reductant inlet 6 near the bottom, and an oxygen sensor 17, a temperature sensor 18 and a pressure sensor 19 are arranged above the reduction zone reductant inlet 6 .

Perforated plates 16 are respectively inclined in the vicinity of the inlet of the flue gas in the adsorption zone and near the inlet of the reducing agent in the reduction zone, and the aperture of the perforated plate 16 is smaller than the particle size of the catalyst. The two sides of the perforated plate 16 are fixedly connected to the side walls of the inner circulating fluidized bed reactor 10, the top of the perforated plate 16 is fixedly connected to the side wall above the flue gas inlet or the reducing agent inlet of the inner circulating fluidized bed reactor 10, and the bottom end is The tops of the side walls of the catalyst collection chamber 12 are fixedly connected, and each connection is completely sealed.

The porous plates 16 of the adsorption zone 22 and the reduction zone 23 and the side walls of the catalyst collection chamber 12 and the side walls and bottom surfaces of the inner circulating fluidized bed reactor 10 respectively enclose two elemental sulfur collection chambers 11 located on both sides of the catalyst collection chamber 12 independently. . The elemental sulfur collection chamber 11 is provided with an elemental sulfur discharge valve 15 on the bottom surface.

A catalyst collection valve 14 is provided on the top surface of the catalyst collection chamber 12, and a catalyst discharge valve 13 is provided on the bottom surface.

Heat exchanger 9 is used for heat exchange of flue gas and reducing agent. The flue gas enters the heat exchanger 9 from the flue gas inlet 2, flows out from the flue gas outlet 4, and enters the flue gas inlet 5 of the adsorption zone. The reductant enters the heat exchanger from the reductant inlet 1, flows out from the reductant outlet 3, and enters the reductant inlet 6 of the reduction zone.

Using the above-mentioned integrated desulfurization and denitrification device with an internal circulating fluidized bed coupled with a heat exchanger to carry out integrated desulfurization and denitrification, the technological process includes the steps:

(1) The high temperature flue gas and reducing agent containing SO ₂ and NO _x are both 200-300 °C after heat exchange in the heat exchanger 9, and then enter the adsorption zone 22 and the reduction zone 23 respectively, and the flue gas passes through the adsorption zone. The catalyst in 22 is then discharged through the flue gas outlet 7, while SO ₂ and NO _x are in contact with the catalyst in the adsorption zone 22 and are adsorbed;

(2) The catalyst adsorbed with SO ₂ and NO _x in the adsorption zone 22 is driven by the airflow and enters the reduction zone 23 across the partition 20 according to the circulating flow direction 8 of the granular catalyst, and the SO ₂ and NO _x adsorbed on the surface of the catalyst are entered The reducing agent in the reduction zone 23 is reduced to liquid elemental sulfur and gaseous N ₂ , the elemental sulfur enters the elemental sulfur collection chamber 11 through the porous plate 16 , and the N ₂ flows back to the adsorption zone 22 and the incoming smoke along with the air flow through the gap under the separator 20 . After the gas is mixed, it is discharged from the flue gas outlet 7;

(3) Driven by the airflow, the catalyst that has undergone the reduction reaction, the surface SO ₂ and NO _x desorption is completely desorbed, and flows back to the adsorption zone through the gap below the separator 20 to enter the next round of SO ₂ and NO _x adsorption;

(4) Circulation steps (1) to (3), realize the integrated desulfurization and denitrification of the inner circulating fluidized bed coupled with the heat exchanger.

The application of integrated desulfurization and denitrification using the above-mentioned internal circulating fluidized bed coupled heat exchanger integrated desulfurization and denitrification device is as follows:

Application example 1

_The flue gas flow is 50L/min, the temperature is 380℃, the SO2 concentration is 500ppm, the _NOx concentration is 500ppm, and the oxygen content is about 8vol%. %), the residence time of the flue gas in the adsorption zone is 18s, and after contacting and adsorbing with the catalyst loaded in the adsorption zone, the catalyst moves to the reduction zone (oxygen concentration 3vol%). The reducing gas is a mixture of hydrogen and nitrogen, the flow rate is 40L/min, the temperature is 250°C, the hydrogen concentration is 0.05vol%, and the temperature is raised to 300°C through a heat exchanger, the residence time of the reducing agent in the reduction zone is 6s, _SO2 and _NOx removal rates were 75% and 80%, respectively.

Application example 2

The flue gas flow rate is 75L/min, the temperature is 380℃, the SO2 concentration is 500ppm, the _NOx concentration is 500ppm, and the oxygen content is about _8.7vol %. 8.7vol%), the residence time of the flue gas in the adsorption zone was 12s, and after contacting and adsorbing with the catalyst loaded in the adsorption zone, the catalyst moved to the reduction zone (oxygen concentration 3.2vol%). The reducing gas is a mixture of hydrogen and nitrogen, the flow rate is 50L/min, the temperature is 250℃, the hydrogen concentration is 0.05vol%, the temperature is raised to 300℃ through a heat exchanger, the residence time of the reducing agent in the reducing zone is 4.8s, the SO2 The removal rates of ₂ and _NOx were 72% and 75%, respectively.

Application example 3

The flue gas flow rate is 75L/min, the temperature is 380℃, the SO2 concentration is 400ppm, the _NOx concentration is 400ppm, and the oxygen content is about _8.5vol %. 8.5vol%), the residence time of the flue gas in the adsorption zone is 12s, and after contacting and adsorbing with the catalyst loaded in the adsorption zone, the catalyst moves to the reduction zone (oxygen concentration 3.5vol%). The reducing gas is a mixture of hydrogen and nitrogen, the flow rate is 40L/min, the temperature is 250°C, the hydrogen concentration is 0.05vol%, and the temperature is raised to 300°C through a heat exchanger, the residence time of the reducing agent in the reduction zone is 6s, _SO2 and _NOx removal rates were 71% and 73%, respectively.

Application example 4

The flue gas flow rate is 75L/min, the temperature is 380℃, the SO2 concentration is 500ppm, the _NOx concentration is 500ppm, and the oxygen content is about _8.2vol %. 8.2vol%), the residence time of the flue gas in the adsorption zone is 12s, and after contacting and adsorbing with the catalyst loaded in the adsorption zone, the catalyst moves to the reduction zone (oxygen concentration 2.5vol%). The reducing gas is a mixture of hydrogen and nitrogen, the flow rate is 75L/min, the temperature is 250℃, the hydrogen concentration is 0.05vol%, and the temperature is raised to 300℃ through a heat exchanger. The residence time of the reducing agent in the reducing zone is 3.2s, the SO2 The removal rates of ₂ and _NOx were 78% and 83%, respectively.

Application example 5

The flue gas flow rate is 75L/min, the temperature is 380℃, the SO2 concentration is 500ppm, the _NOx concentration is 500ppm, and the oxygen content is about _8.2vol %. 8.2vol%), the residence time of the flue gas in the adsorption zone is 12s, and after contacting and adsorbing with the catalyst loaded in the adsorption zone, the catalyst moves to the reduction zone (oxygen concentration 2.5vol%). The reducing gas is a mixture of CO and nitrogen, the flow rate is 75L/min, the temperature is 250 °C, the CO concentration is 0.1 vol%, and the temperature is raised to 300 °C through a heat exchanger, the residence time of the reducing agent in the reduction zone is 3.2s, SO The removal rates of ₂ and _NOx were 75% and 80%, respectively.

In addition, it should be understood that after reading the above description of the present utility model, those skilled in the art can make various changes or modifications to the present utility model, and these equivalent forms also fall within the scope defined by the appended claims of the present application.

Claims (7)

1. The utility model provides an internal circulation fluidized bed coupling heat exchanger integration SOx/NOx control device which characterized in that includes:

the heat exchanger is used for heat exchange between the flue gas and the reducing agent;

the internal circulation fluidized bed reactor with the catalyst is provided with a flue gas outlet at the top, an adsorption area and a reduction area which are circularly communicated are divided by a vertical partition plate inside, a side wall opening of the adsorption area close to the bottom is connected with the flue gas outlet of the heat exchanger, a side wall opening of the reduction area close to the bottom is connected with a reducing agent outlet of the heat exchanger, porous plates for uniformly distributing gas are arranged at a flue gas inlet of the adsorption area and a reducing agent inlet of the reduction area, and oxygen sensors, temperature sensors and pressure sensors are arranged on the side walls of the adsorption area and the reduction area.

2. The integrated desulfurization and denitrification device of the internal circulation fluidized bed-coupled heat exchanger as claimed in claim 1, wherein the volume ratio of the adsorption zone to the reduction zone is 3-5: 1.

3. The integrated desulfurization and denitrification device of claim 1 or 2, wherein a catalyst collection chamber is arranged in the middle of the inner bottom of the internal circulating fluidized bed reactor and is positioned below the adsorption zone and the reduction zone, a catalyst collection valve is arranged on the top surface of the catalyst collection chamber, and a catalyst discharge valve is arranged on the bottom surface of the catalyst collection chamber.

4. The integrated desulfurization and denitrification device of claim 3, wherein the ratio of the distance between the top end of the partition plate and the top surface of the internal circulating fluidized bed reactor to the height of the internal circulating fluidized bed reactor is 3-6: 100;

the ratio of the distance between the bottom end of the partition plate and the top surface of the catalyst collecting chamber to the height of the internal circulating fluidized bed reactor is 3-6: 100.

5. The integrated desulfurization and denitrification device of claim 3, wherein the bottom end of the porous plate is fixedly connected with the side wall of the catalyst collecting chamber, the top end of the porous plate is fixedly connected with the side wall of the internal circulating fluidized bed reactor, and the porous plate, the side wall of the catalyst collecting chamber, and the side wall and the bottom surface of the internal circulating fluidized bed reactor enclose an elemental sulfur collecting chamber;

and the bottom surface of the elemental sulfur collection chamber is provided with an elemental sulfur discharge valve.

6. The integrated desulfurization and denitrification device of claim 1, wherein the ratio of the mass of the catalyst to the volume of the internal circulation fluidized bed reactor is 20-40 kg:1m³。

7. The integrated desulfurization and denitrification device of claim 1, wherein the top surface of the adsorption zone is provided with a catalyst feeding valve.

Images