CN114471108B - Synchronous decarbonization denitration of industry flue gas and waste heat recovery utilize's device - Google Patents

Abstract

The invention provides a device for synchronous decarbonization, denitration and waste heat recovery of industrial flue gas, which comprises: the device comprises a decarburization denitration tower, ammonia spraying equipment and a reaction bed layer, wherein the decarburization denitration tower is provided with a flue gas inlet and a flue gas outlet, the inside of the decarburization denitration tower is provided with a plurality of reaction bed layers, the reaction bed layers are located between the flue gas inlet and the flue gas outlet, a heat exchange inlet and a first heat exchange outlet are arranged on the side wall of the decarburization denitration tower, an ammonia water inlet is arranged on the side wall of the decarburization denitration tower, the ammonia spraying equipment is arranged in the decarburization denitration tower, and the ammonia water inlet is communicated with the ammonia spraying equipment. The technical scheme of the invention can dynamically adjust the arrangement in the decarburization and denitration tower according to the temperature of the flue gas, and perform decarburization and denitration simultaneously in the decarburization and denitration tower, thereby greatly saving the equipment investment of step-by-step treatment, reducing the occupied area and saving the cost and the operating cost.

Description

A device for synchronous decarbonization and denitrification of industrial flue gas and recovery of waste heat

technical field

The invention relates to the field of industrial flue gas treatment, in particular to a device for synchronous decarbonization and denitrification of industrial flue gas and waste heat recovery and utilization.

Background technique

At present, in the process of industrial production, a large amount of harmful gases are produced. In addition to SO ₂ , CO and NO _X also seriously pollute the environment and affect people's normal life.

In view of the diversity of pollution components in industrial waste gas and the further development and application of multi-pollutant synchronous removal technology, synchronous decarbonization and denitrification are receiving extensive attention and research from all walks of life. Advance relevant research and applications. However, in the same tower body, in the process of synchronous decarburization and denitrification, due to the difference in the reaction temperature range between the two, the sharp rise in the temperature of the denitrification bed in the denitrification process and the excessive oxidation of the reducing agent ammonia, etc. As a result, the denitrification activity has dropped significantly, resulting in outlet NO _X emissions not up to the standard. Therefore, in the process of synchronous decarbonization and denitrification, the excess heat generated by the decarburization bed is fully recycled to make the denitrification bed efficient. The technical demand for denitrification is imminent.

In view of the above reasons, a device for synchronous decarbonization and denitrification of industrial flue gas and waste heat recovery and utilization is needed.

Contents of the invention

The purpose of the present invention is to provide a device for synchronous decarbonization and denitration of industrial flue gas and waste heat recovery and utilization. The reaction beds achieve high decarburization activity at their respective suitable operating temperatures, and at the same time, the excess heat of the decarburization bed can also be used in various applications.

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

A device for synchronous decarbonization and denitration of industrial flue gas and waste heat recovery and utilization, the device includes: a decarbonization and denitrification tower, ammonia injection equipment and a reaction bed, wherein the decarbonization and denitrification tower has a flue gas inlet and a flue gas outlet , a plurality of reaction beds are arranged in the decarbonization and denitrification tower, and the plurality of reaction beds are all located between the flue gas inlet and the flue gas outlet, and the side of the decarbonization and denitrification tower A heat exchange inlet and a first heat exchange outlet are arranged on the wall, an ammonia water inlet is arranged on the side wall of the decarbonization and denitrification tower, the ammonia injection equipment is arranged in the decarbonization and denitration tower, and the ammonia water inlet is connected to the The above-mentioned ammonia injection equipment is connected.

Further, in the above-mentioned device for synchronous decarbonization and denitrification of industrial flue gas and waste heat recovery and utilization, it also includes a circulation pipeline and a liquid storage tank, the tower wall of the decarbonization and denitrification tower is provided with an interlayer, and the circulation pipeline Arranged in the interlayer, the two ends of the circulation pipeline communicate with the liquid storage tank through the heat exchange inlet and the first heat exchange outlet, and part of the bottom of the reaction bed is provided with a disc-shaped tube, the coiled tube is in direct contact with the catalyst material filled in the reaction bed, and all the coiled tubes in the decarburization and denitrification tower are connected in sequence through the circulation pipeline. The carbon denitrification tower is provided with a plurality of split grid tubes, and the inlet and outlet of the split grid tubes are connected with the circulation pipeline; the side wall of the decarburization and denitrification tower is provided with a first gas detection port, A first gas detection device is connected to the first gas detection port, and a plurality of temperature detection points are arranged in the decarbonization and denitrification tower, and the temperature detection points are connected with the first temperature set outside the decarbonization and denitrification tower. The device is connected; preferably, the interlayer is filled with thermal insulation material.

Further, in the above-mentioned device for synchronous decarbonization and denitrification of industrial flue gas and waste heat recovery and utilization, a liquid level gauge is provided on the side wall of the liquid storage tank, and a liquid injection port and a drain are provided on the top of the liquid storage tank. A pressure port, a drain valve is provided at the bottom of the liquid storage tank, and an output pump is provided on the pipeline between the liquid storage tank and the heat exchange inlet.

Further, in the above-mentioned device for synchronous decarbonization and denitrification of industrial flue gas and waste heat recovery and utilization, the ammonia injection equipment includes an ammonia water pipeline and an atomizing nozzle, and the ammonia water pipeline is used to connect the ammonia water inlet to the The atomizing nozzles are connected, and the first heat exchange outlet is arranged downstream of all the reaction beds.

Further, in the above-mentioned device for synchronous decarbonization and denitration of industrial flue gas and waste heat recovery and utilization, the flue gas inlet is located at the top of the decarbonization and denitrification tower, and a flue gas pipeline is connected to the flue gas inlet, and the flue gas inlet is connected to the flue gas inlet. The flue gas outlet is located at the bottom of the decarbonization and denitrification tower, and the flue gas outlet is connected with a discharge pipe. The flue gas enters the decarbonization and denitrification tower from the flue gas inlet, and passes through the discharge pipe from the flue gas outlet. For discharge, a second temperature device and a second gas detection port are provided on the discharge pipe, and a second gas detection device is connected to the second gas detection port.

Further, in the above-mentioned device for synchronous decarbonization and denitrification of industrial flue gas and waste heat recovery and utilization, the carbon refers to CO, the nitrogen refers to _NOx , and the flue gas entering the decarbonization and denitrification tower from the flue gas inlet The concentration of CO in the medium is 0-15000 mg/Nm ³ , and the concentration of NO _X is 0-1000 mg/Nm ³ , and the catalyst materials in the reaction bed are all formed catalysts.

Further, in the above-mentioned device for synchronous decarbonization and denitrification of industrial flue gas and recovery of waste heat, if the temperature of the flue gas at the inlet of the flue gas is 100°C to 180°C, the reaction bed includes a decarburization bed and denitrification beds, a plurality of the decarburization beds and a plurality of the denitrification beds are arranged sequentially from the flue gas inlet to the flue gas outlet, and the heat exchange inlet is arranged at the first decarbonization bed bed, the ammonia injection equipment is arranged upstream of the first denitrification bed, a plurality of the split grid pipes are respectively arranged upstream of the decarburization beds from top to bottom, A second heat exchange outlet is arranged on the side wall of the decarburization and denitration tower between each of the decarburization beds and the plurality of denitration beds, and the circulation pipeline and the second heat exchange outlet are both The second heat exchange outlet is connected with a heating pipe and a return pipe, the return pipe is connected with the liquid storage tank, the heating pipe passes through the flue gas pipe, and the heating pipe is used to heat the smoke entering the Inlet flue gas.

Further, in the above-mentioned device for synchronous decarbonization and denitrification of industrial flue gas and waste heat recovery and utilization, if the temperature of the flue gas at the inlet of the flue gas is 180°C to 240°C, the reaction bed includes a decarburization bed and denitration beds, a plurality of denitrification beds and a plurality of decarburization beds are arranged sequentially from the flue gas inlet to the flue gas outlet, and the heat exchange inlet is arranged at the first decarbonization bed The ammonia injection equipment is arranged upstream of the first denitrification bed, and the plurality of split grid pipes are respectively arranged upstream of the plurality of decarburization beds from top to bottom.

Further, in the above-mentioned device for synchronous decarbonization and denitrification of industrial flue gas and recovery of waste heat, if the temperature of the flue gas at the inlet of the flue gas is 240°C to 280°C, the reaction bed includes a denitrification and decarburization bed layer, from the flue gas inlet to the flue gas outlet, a plurality of the denitrification and decarburization beds are sequentially arranged, the heat exchange inlet is arranged upstream of the first denitrification and decarbonization bed, and the ammonia injection The equipment is arranged upstream of the first denitrification and decarburization bed, and a plurality of the split grid pipes are respectively arranged upstream of the plurality of denitrification and decarbonization beds from top to bottom.

Further, in the above-mentioned device for synchronous decarbonization and denitrification of industrial flue gas and waste heat recovery and utilization, it also includes a two-way valve, when the decarbonization and denitrification tower is sequentially provided with When there are multiple decarburization beds and multiple denitrification beds, there are three two-way valves, and the three two-way valves are respectively the first valve, the second valve and the third valve. The first valve is set on the circulation pipeline between the denitrification bed and the decarburization bed, the second valve is set on the heating pipe, and the third valve is set on the return pipe When the flue gas entering from the flue gas inlet needs to be heated and kept warm, the first valve and the third valve are closed, the second valve is opened, and the circulating fluid absorbs the heat of the decarburization bed Finally, the flue gas in the flue gas pipeline can be heated through the heating pipe, and when the temperature of the denitration bed layer is lower than the denitration catalytic activation temperature, the second valve and the third valve are closed, When the first valve is opened, the circulating fluid can heat the denitrification bed after absorbing the heat of the decarburization bed. When heating and heat preservation are required, close the first valve and the second valve, open the third valve, and the circulating fluid will flow back to the liquid storage tank through the return pipe after absorbing the heat of the decarburization bed .

Analysis shows that the present invention discloses a device for synchronous decarbonization and denitrification of industrial flue gas and waste heat recovery and utilization. The device can decarbonize and denitrify industrial flue gas synchronously and recycle waste heat generated in the decarbonization process. Compared with the prior art, the technical solution of the present invention simultaneously performs decarbonization and denitrification in the decarbonization and denitrification tower, which can greatly save equipment investment for step-by-step treatment, reduce floor space, and save costs and operating expenses. The present invention effectively recovers the excess heat generated by decarbonization, which can effectively ensure the normal operation of denitrification. At the same time, the recovered heat can also be used to heat or keep warm the flue gas entering from the flue gas inlet, which can reduce the heating of the flue gas. The investment in equipment keeps the temperature of the imported flue gas stable, which is conducive to decarbonization. The invention can not only decarburize and denitrify synchronously, but also use the waste heat for other purposes according to the actual situation, so as to achieve double benefit effects.

Description of drawings

The exemplary embodiments and descriptions of the present invention are used to explain the present invention, and do not constitute an improper limitation of the present invention. in:

Figure 1 is a schematic structural diagram of an embodiment of the present invention (decarburization first and then denitrification).

Fig. 2 is a schematic structural view of a coiled tube according to an embodiment of the present invention.

Fig. 3 is a schematic diagram of the arrangement of coiled tubes in a reaction bed according to an embodiment of the present invention.

Fig. 4 is a schematic structural diagram of a distribution grid tube according to an embodiment of the present invention.

Fig. 5 is a schematic structural diagram of a decarburization and denitrification tower according to an embodiment of the present invention (first denitration and then decarburization).

Fig. 6 is a schematic structural diagram of a decarbonization and denitration tower according to an embodiment of the present invention (simultaneous decarbonization and denitrification).

Explanation of reference signs: 1 decarbonization and denitrification tower; 2 reaction bed; 3 decarbonization bed; 4 denitration bed; 5 denitration and decarbonization bed; 6 flue gas inlet; 7 flue gas outlet; 1st heat exchange outlet; 10 ammonia water inlet; 11 ammonia water pipeline; 12 atomizing nozzle; 13 circulation pipeline; 14 liquid storage tank; 1 gas detection device; 19 temperature detection point; 20 first temperature device; 21 liquid level gauge; 22 liquid injection port; 23 pressure relief port; 24 liquid discharge valve; 25 output pump; 26 discharge pipe; 28 second gas detection port; 29 first valve; 30 second valve; 31 third valve; 32 heating pipe; 33 return pipe; 34 flue gas pipe; 35 second heat exchange outlet.

detailed description

The present invention will be described in detail below with reference to the accompanying drawings and examples. Each example is provided by way of explanation of the invention, not limitation of the invention. In fact, those skilled in the art will recognize that modifications and variations can be made in the present invention without departing from the scope or spirit of the invention. For example, features illustrated or described as part of one embodiment can be used on another embodiment to yield a still further embodiment.

In the description of the present invention, the terms "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", " The orientations or positional relationships indicated by "top", "bottom", etc. are based on the orientations or positional relationships shown in the drawings, and are only for the convenience of describing the present invention and do not require that the present invention must be constructed and operated in a specific orientation, so they cannot be understood as Limitations on the Invention. The terms "connected", "connected" and "set" used in the present invention should be understood in a broad sense, for example, they can be fixedly connected or detachably connected; they can be directly connected or indirectly connected through intermediate parts; It may be a wired electrical connection, a wireless connection, or a wireless communication signal connection, and those skilled in the art can understand the specific meanings of the above terms according to specific situations.

One or more examples of the invention are illustrated in the accompanying drawings. The detailed description uses numerical and letter designations to refer to features in the drawings. Like or analogous numerals in the drawings and description have been used to refer to like or analogous parts of the present invention. As used herein, the terms "first," "second," and "third," etc., are used interchangeably to distinguish one element from another and are not intended to denote the location or importance of individual elements. .

As shown in Figures 1 to 6, according to an embodiment of the present invention, a device for synchronous decarbonization and denitrification of industrial flue gas and recovery of waste heat is provided, the device includes: decarbonization and denitrification tower 1, ammonia injection equipment and a reaction bed Layer 2, wherein, the embodiment of the present invention takes the decarbonization and denitrification tower 1 as a cylindrical tower body structure as an example for introduction. The decarbonization and denitrification tower 1 can also adopt other shapes such as a square tower body according to the actual situation. The decarbonization and denitrification tower 1 It has a flue gas inlet 6 and a flue gas outlet 7, and a flue gas pipe 34 is connected to the flue gas inlet 6. The industrial flue gas enters the decarbonization and denitrification tower 1 after passing through the flue gas pipe 34 and the flue gas inlet 6 in sequence. 1 is provided with a plurality of reaction beds 2, and the plurality of reaction beds 2 are located between the flue gas inlet 6 and the flue gas outlet 7. The industrial flue gas enters through the flue gas inlet 6 and flows through the plurality of reaction beds 2. Discharged from the flue gas outlet 7, the industrial flue gas undergoes synchronous decarburization and denitration during the process of flowing through multiple reaction beds 2. In the technical solution of the present invention, there is no limit to the number of layers of the reaction bed 2 used for decarburization, denitrification or simultaneous decarburization and denitrification, and the number of layers of the reaction bed 2 can be determined according to the actual situation. The side wall of the decarbonization and denitrification tower 1 is provided with a heat exchange inlet 8 and a first heat exchange outlet 9, the side wall of the decarbonization and denitration tower 1 is provided with an ammonia water inlet 10, and the ammonia injection equipment is arranged in the decarbonization and denitration tower 1, The ammonia water inlet 10 is connected with the ammonia spraying equipment, which can spray ammonia water, and the ammonia water is atomized to reduce NO _x in the flue gas under the action of the catalyst material. During the decarbonization process, CO is oxidized to CO ₂ to release excess heat and heat the flue gas. If this part of the heat is not used, it will cause waste of heat and affect denitrification. The heated flue gas flows into the denitrification bed layer 4 to make denitrification The bed 4 is heated up, and when the temperature of the denitration bed 4 exceeds the normal operating temperature of the denitration catalyst, the denitration effect will be deteriorated. The technical solution of the present invention can not only realize good control of the heating amount of the denitrification bed 4 , ensure the normal progress of the denitrification reaction of the denitrification bed 4 , but also realize resource utilization of excess heat of the decarburization bed 3 .

Further, in the technical solution of the present invention, carbon refers to CO and nitric acid refers to NO _X . The CO concentration in the flue gas entering the decarbonization and denitrification tower 1 from the flue gas inlet 6 is 0-15000 mg/Nm ³ , and the NO _X concentration is 0 ~1000mg/Nm ³ , the catalyst materials in the reaction bed layer 2 are all shaped catalysts. The decarbonization and denitrification tower 1 will generate waste heat during the decarburization process. The amount of waste heat utilization depends on the temperature rise of the decarburization bed 3 brought about by the heat released by the catalytic oxidation of CO during the actual decarbonization reaction process. Among them, the catalytic oxidation of CO The temperature increase △T of the flue gas is:

△T=

According to the CO catalytic oxidation process, there are:

W＝Q·C·f·η

f＝a·GHSV+k

GHSV=Q/V

Get: △T=

Among them: Q: flue gas flow rate; Cp: flue gas specific heat capacity; △T: flue gas temperature change before and after CO catalytic oxidation in the decarburization bed; f: CO catalytic oxidation conversion rate; The relationship constant of CO catalytic oxidation conversion rate is a negative value; k is the reaction constant of the space velocity in the decarbonization and denitrification tower and the CO catalytic oxidation conversion rate, which is a positive value; GHSV: decarbonization and denitrification tower space velocity, GHSV∈[2000, 20000]; V: decarbonization catalyst loading in the decarbonization and denitrification tower; W: heat production of the decarbonization bed in the decarbonization and denitration tower; C: _CO concentration in the flue gas; of heat release.

CO(g)+1/2O ₂ (g)=CO ₂ (g) △H=-283.0KJ/mol

进行计算得到脱碳床层3的CO催化氧化前后烟气温度的变化约127.3℃，即烟气会由于CO催化氧化实现理论升温约127.3℃，所以具有烟气余热利用价值。Take CO concentration of 15000mg/Nm ³ , flow rate of Qm ³ /h, catalyst of 1m ³ , space velocity of 5000h ^-1 , flue gas specific heat capacity of about 1.2KJ/m ³ •°C, complete catalytic oxidation of CO (conversion rate 100%) as an example , then 283.0KJ of heat can be released according to the oxidation of 1mol CO into CO ₂ , then 15000mg/Nm ³ ie 0.54mol/Nm ³ can release 152.8KJ/Nm ³ of heat, and CO can be converted into CO ₂ under the flow rate of Qm ³ /h When the heat release is 152.8*QKJ/h, then through the above formula △T=

Calculation shows that the change of flue gas temperature before and after CO catalytic oxidation in decarburization bed 3 is about 127.3°C, that is, flue gas will achieve a theoretical temperature rise of about 127.3°C due to CO catalytic oxidation, so it has the value of flue gas waste heat utilization.

Further, the device also includes a circulation pipeline 13 and a liquid storage tank 14. The tower wall of the decarbonization and denitrification tower 1 is provided with an interlayer, and the circulation pipeline 13 is arranged in the interlayer. The circulation pipeline 13 needs to have certain high temperature resistance, Corrosion resistance and pressure resistance and other characteristics, the pipe diameter of the circulation pipeline 13 can be determined according to the actual application situation, and the interlayer is also filled with insulation cotton or other insulation materials for the insulation of the decarbonization and denitrification tower 1. Both ends of the circulation pipeline 13 communicate with the liquid storage tank 14 through the heat exchange inlet 8 and the first heat exchange outlet 9 respectively, and a coiled tube 15 is arranged at the bottom of part of the reaction bed 2, and the material of the coiled tube 15 is corrosion-resistant High temperature resistant stainless steel, the coiled tube 15 is in direct contact with the catalyst material filled in the reaction bed 2, all the coiled tubes 15 in the decarburization and denitrification tower 1 are connected in turn through the circulation pipeline 13, and the circulation pipeline 13 When the circulating liquid flows through the coiled tube 15 of the decarburization bed 3 or the denitrification and decarburization bed 5, the excess heat generated by the catalyst material during the decarburization process can be recovered in situ, and the circulating liquid in the circulation line 13 flows through The denitrification bed layer 4 can heat the catalyst material in situ to ensure the denitrification effect. As shown in Figure 2 and Figure 3, a coiled tube 15 is in the same plane and is in a spiral shape as a whole. The spiral coiled tube 15 leaves enough space to ensure the normal circulation of smoke. The shape, size and pipe diameter are not fixed, but can be determined according to the size of the space of the reaction bed 2 in the actual decarbonization and denitrification tower 1 and the effect of heat exchange. In the decarbonization and denitrification tower 1, a plurality of distribution grid tubes 16 are arranged, and the inlet and outlet of the distribution grid tubes 16 are connected with the circulation pipeline 13. The material of the distribution grid tubes 16 is corrosion-resistant and high-temperature-resistant stainless steel. The tower wall of the carbon denitrification tower 1 is provided with buckles, and the diversion grid tube 16 is arranged upstream of the decarbonization bed 3 through the buckle. The diversion grid tube 16 is in direct contact with the flue gas. In order to make the flue gas circulate normally, the diversion The grid tube 16 leaves enough gaps, and when the circulating fluid in the circulation line 13 flows through the diversion grid tube 16, it not only achieves in-situ recovery of the CO produced by the massive oxidation of the decarburization bed 3 during the decarburization process Excess heat, and can well divert the imported flue gas, while avoiding increasing the flow resistance of the flue gas, so that the flue gas can flow smoothly, and then the catalyst material can fully contact and react with the flue gas. The present invention does not limit the shape of the distribution grid tube 16. In one embodiment of the present invention, as shown in FIG. A plurality of vertical pipes are sequentially arranged above the several horizontal pipes, and the several horizontal pipes are connected in sequence to communicate with the sequentially connected vertical pipes. In other embodiments of the present invention, the distribution grid tube 16 may also have other shapes. The side wall of the decarbonization and denitrification tower 1 is provided with a first gas detection port 17, and a first gas detection device 18 is connected to the first gas detection port 17. The first gas detection port 17 is used to detect the smoke in the decarbonization and denitrification tower 1. The concentration of CO, CO ₂ , NO _X (NO, NO ₂ ) in the gas is used to determine the oxidation of CO and the removal of NO _X in the actual application process. For example, compared with the concentration value of the imported flue gas, If the _CO2 concentration in the decarbonization and denitrification tower 1 or the flue gas outlet 7 is high and the _NOx concentration is low, it means that the degree of CO oxidation is relatively high, the decarbonization effect is relatively good, the _NOx removal rate is relatively high, and the denitration rate is relatively high. The effect is better. The decarbonization and denitrification tower 1 is provided with a plurality of temperature detection points 19, and the temperature detection points 19 are connected with the first temperature device 20 arranged outside the decarbonization and denitrification tower 1, and the decarburization and denitrification reactions are simultaneously carried out in the decarbonization and denitrification tower 1 The first gas detection device 18 and the first temperature device 20 can constantly detect the temperature in the decarbonization and denitrification tower 1 and the contents of CO and NO _x in the flue gas. According to the detection results of the temperature of each temperature detection point 19 in the decarbonization and denitrification tower 1 by the first temperature device 20, the flow direction of the circulating fluid is determined. By changing the flow direction of the circulating fluid, the flue gas in the flue gas pipeline 34 can be heated and Insulation, or the purpose of heating the catalyst material in the denitrification bed layer 4 .

Further, the liquid storage tank 14 is a box for storing a certain volume of circulating liquid, wherein the circulating liquid can be suitable material components such as water or heat transfer oil, and the circulating liquid circulates between the decarbonization and denitrification tower 1 and the liquid storage tank 14 , capable of absorbing the heat generated by the catalyst material in the decarbonization and denitrification tower 1 during the decarburization process and recycling it. A liquid level gauge 21 is arranged on the side wall of the liquid storage tank 14. The liquid level gauge 21 is used to monitor the liquid level of the circulating fluid in the liquid storage tank 14. The top of the liquid storage tank 14 is provided with a liquid injection port 22 and a pressure relief port. 23. The liquid injection port 22 is used to replenish circulating fluid to the liquid storage tank 14, and the pressure relief port 23 is used to release the excess pressure in the liquid storage tank 14 to ensure the normal operation of the device. The bottom of the liquid storage tank 14 is provided with a drain The liquid valve 24 is provided with an output pump 25 on the pipeline between the liquid storage tank 14 and the heat exchange inlet 8, and the circulation pipeline 13 is connected with the output pump 25 through the heat exchange inlet 8, and the output pump 25 is used to transfer the circulating fluid smoothly Send it into the internal circulation pipeline 13 of the decarbonization and denitrification tower 1, and realize circulation. The circulation pipeline 13 in the decarbonization and denitrification tower 1 is respectively connected with the split grid pipe 16 and the coil pipe 15, and according to whether it is necessary to provide heating and heat preservation to the flue gas entering the flue gas inlet 6 and whether it is necessary to provide a denitrification bed 4, the catalyst material is heated and kept warm, and the final circulating liquid has three flow directions, one is to flow to the flue gas pipeline 34 connected to the flue gas inlet 6, the other is to flow to the denitrification bed 4, and the third is to directly flow back to the liquid storage tank 14. Which flow direction to choose can be determined according to the actual reaction temperature requirements. After the circulating fluid absorbs heat, the liquid storage tank 14 is used to store the heat. The liquid storage tank 14 can also be connected to and supply heat to other equipment that needs heat supply, so as to realize the recovery and utilization of waste heat.

Further, the ammonia injection equipment includes an ammonia water pipeline 11 and an atomizing nozzle 12, the ammonia water pipeline 11 is used to communicate the ammonia water inlet 10 with the atomizing nozzle 12, the atomizing nozzle 12 can spray ammonia water and atomize the ammonia water, and the ammonia water mist After denitrification, fully contact with the catalyst material used for denitrification, and reduce the _NOx in the flue gas under the action of the catalyst material. The first heat exchange outlet 9 is arranged downstream of all the reaction beds 2, and the circulating liquid is in the decarburization and denitrification tower 1 The flow direction inside is from top to bottom, which can reduce the resistance of circulating fluid flow.

Further, the flue gas inlet 6 is located at the top of the decarbonization and denitrification tower 1, the flue gas outlet 7 is located at the bottom of the decarbonization and denitrification tower 1, and the flue gas outlet 7 is connected with a discharge pipe 26, and the flue gas enters the decarbonization and denitrification tower from the flue gas inlet 6. Tower 1 is discharged from the flue gas outlet 7 through the discharge pipe 26. A second temperature device 27 and a second gas detection port 28 are arranged on the discharge pipe 26, and a second gas detection device is connected to the second gas detection port 28. The second temperature device 27 and the second gas detection device can detect the temperature of the flue gas discharged from the flue gas outlet 7 and the contents of CO and NO _x .

Further, if the temperature of the flue gas at the flue gas inlet 6 is 100°C to 180°C, as shown in Figure 1, the reaction bed 2 includes a decarburization bed 3 and a denitrification bed 4, and the flue gas passes through the decarbonization and denitrification tower 1 The sequence of internal decarburization and denitrification is first decarburization and then denitrification. Multiple decarburization beds 3 and multiple denitrification beds 4 are arranged in sequence from the flue gas inlet 6 to the flue gas outlet 7. The heat exchange inlet 8 is set at the first denitrification bed. Upstream of the carbon bed 3, the atomizing nozzle 12 of the ammonia spraying equipment is set upstream of the first denitrification bed 4, that is: the atomizing nozzle 12 of the ammonia spraying equipment is set on both the decarbonization bed 3 and the denitration bed 4 In the middle of the gap between them, this setting can prevent the ammonia water sprayed out by the atomizing nozzle 12 from being over-oxidized by the high-temperature flue gas in the decarburization bed 3, and can also make the ammonia water atomized and fully mixed with the catalyst material in the denitrification bed 4. Contact to ensure the effect of denitrification. A plurality of split grid tubes 16 are respectively arranged upstream of multiple decarburization beds 3 from top to bottom. In one embodiment of the present invention, two split grid tubes 16 are provided, and two split grid tubes 16 They are arranged upstream of the first decarbonization bed 3 and the second decarburization bed 3 respectively, and are arranged on the side wall of the decarburization and denitrification tower 1 between multiple decarbonization beds 3 and multiple denitrification beds 4 There is a second heat exchange outlet 35, the circulation pipeline 13 is connected with the second heat exchange outlet 35, the second heat exchange outlet 35 is connected with a heating pipe 32 and a return pipe 33, the return pipe 33 is connected with the liquid storage tank 14, and the heating pipe 32 passes through the flue gas pipe 34, and the heating pipe 32 is used to heat the flue gas entering the flue gas inlet 6 from the flue gas pipe 34.

Further, if the temperature of the flue gas at the flue gas inlet 6 is 180°C to 240°C, the reaction bed 2 includes a decarburization bed 3 and a denitrification bed 4, and the flue gas is decarbonized and denitrated in the decarbonization and denitrification tower 1. The sequence is denitrification first and then decarbonization. Multiple denitrification beds 4 and multiple decarbonization beds 3 are arranged sequentially from the flue gas inlet 6 to the flue gas outlet 7, and the heat exchange inlet 8 is set at the first decarbonization bed 3. Upstream, the atomizing nozzle 12 of the ammonia injection equipment is arranged upstream of the first denitrification bed 4, and a plurality of split grid pipes 16 are respectively arranged upstream of the plurality of decarburization beds 3 from top to bottom. In one embodiment, as shown in FIG. 5 , two denitrification beds 4 and four decarburization beds 3 are provided.

Further, if the temperature of the flue gas at the flue gas inlet 6 is 240°C to 280°C, the reaction bed 2 includes a denitrification and decarburization bed 5, and the flue gas is simultaneously decarbonized and denitrified in the decarbonization and denitrification tower 1, and the flue gas From the inlet 6 to the flue gas outlet 7, multiple denitrification and decarbonization beds 5 are arranged in sequence, the heat exchange inlet 8 is arranged upstream of the first denitrification and decarbonization bed 5, and the atomizing nozzle 12 of the ammonia injection equipment is arranged on the first denitrification and decarbonization bed 5. Upstream of the carbon bed 5, a plurality of split grid pipes 16 are respectively arranged upstream of the plurality of denitrification and decarbonization beds 5 from top to bottom. In one embodiment, as shown in FIG. 6 , six denitrification and decarburization beds 5 are provided.

Further, the device also includes a two-way valve, which is a control valve with high temperature resistance, corrosion resistance and flexible operation. The two-way valve is used to control the flow direction of the circulating fluid in the circulation line 13. By opening or closing the two-way valve Finally, the flow direction of the circulating liquid with recovered heat flowing through the decarburization bed 3 is controlled. Depending on whether it is necessary to heat and insulate the flue gas entering the flue gas inlet 6 and whether it is necessary to heat and insulate the catalyst material in the denitrification bed layer 4, the circulating fluid finally has three flow directions, one is to flow to the flue gas connected to the imported flue gas The second one of the pipeline 34 flows to the denitrification bed layer 4, and the third one directly flows back to the liquid storage tank 14. The specific choice of which flow direction can be determined according to the actual reaction temperature requirements.

For the imported flue gas temperature of 180°C ~ 240°C first denitration and then decarburization and 240°C ~ 280°C simultaneous decarbonization and denitrification is based on the device used for the first decarbonization and then denitrification at the inlet flue temperature of 100°C ~ 180°C. The upper and lower positions of the ammonia spraying equipment, the circulation pipeline 13, the coiled pipe 15 and the distribution grid pipe 16 are sufficient.

Example 1:

In this embodiment, the temperature of the flue gas at the 6 flue gas inlets is 100°C to 180°C, and the sequence of decarbonization and denitrification of the flue gas in the decarbonization and denitrification tower 1 is first decarburization and then denitrification, as shown in Figure 1, by From the flue gas inlet 6 to the flue gas outlet 7, there are two decarbonization beds 3 and four denitration beds 4 in sequence. The decarburization bed 3 is filled with a catalyst specially used for decarbonization, and the denitrification bed 4 is filled with a special catalyst for denitrification. catalyst. There are two splitter grid pipes 16, and the two splitter grille pipes 16 are respectively arranged upstream of the two decarburization beds 3, and the atomizing nozzle 12 of the ammonia injection equipment is arranged upstream of the first denitrification bed 4. There are two temperature detection points 19, one temperature detection point 19 is set between the two decarburization beds 3, and the other temperature detection point 19 is set between the second denitration bed 4 and the third denitration bed 4 Between, each temperature detection point 19 is connected with a first temperature device 20 . The first gas detection port 17 is arranged between the first denitration bed 4 and the second denitration bed 4 . The bottoms of the two decarburization beds 3 , the third denitrification bed 4 and the fourth denitrification bed 4 are all provided with coiled tubes 15 , and the coiled tubes 15 in the decarburization bed 3 and the split grid tubes 16 Used to absorb the waste heat generated during the decarburization process, the coiled tube 15 in the denitration bed 4 is used to heat the catalyst material in the denitration bed 4, because the first denitration bed 4 and the second denitration The beds 4 are all close to the decarburization bed 3, although most of the heat can be recovered by using the circulating fluid in the coiled tube 15 of the decarburization bed 3, it will also heat part of the flue gas to heat up the flue gas. When entering the first denitration bed 4 and the second denitration bed 4, the temperature of the flue gas is high enough to ensure the progress of the denitration reaction, the catalyst material does not need to be heated, and the flue gas passes through the third denitration bed 4 and the fourth denitrification bed 4, the flue gas temperature drops, and the lower flue gas temperature does not use denitrification, so there is no need to set a coiled pipe 15 in the first denitrification bed 4 and the second denitrification bed 4 , and coiled tubes 15 need to be set in the third denitration bed 4 and the fourth denitration bed 4 .

In this embodiment, there are three two-way valves, the three two-way valves are respectively the first valve 29, the second valve 30 and the third valve 31, and the first valve 29 is set on the first denitrification bed layer 4 and the second On the circulating pipeline 13 between the two denitrification beds 4, the second valve 30 is arranged on the heating pipe 32, and the third valve 31 is arranged on the return pipe 33. The first temperature device 20 is connected to the first valve 29, the second valve 30 and the third valve 31. The first gas detection port 17 and the first temperature device 20 can transmit feedback. The monitoring value can automatically control the first valve 29 , the second valve 30 and the third valve 31 , and then control the flow direction of the circulating fluid in the circulating pipeline 13 . The first valve 29 , the second valve 30 and the third valve 31 can also be controlled manually according to the gas concentration values detected by the first gas detection port 17 and the second gas detection port 28 , so as to control the flow direction of the circulating fluid. The number and position of the two-way valves are not fixed and can be changed flexibly, but the three flow directions of the final circulating fluid need to remain unchanged.

When the flue gas entering from the flue gas inlet 6 needs to be heated and kept warm, the first valve 29 and the third valve 31 are closed, and the second valve 30 is opened, and the circulating fluid flows out from the liquid storage tank 14 through the output pump 25, and undergoes heat exchange in turn. After the inlet 8, the circulation pipeline 13, the split grid pipe 16, the coiled pipe 15 in the decarburization bed 3 and the second heat exchange outlet 35, it flows to the flue gas pipe 34 through the heating pipe 32, and the circulating fluid absorbs the decarburization bed The heat from the layer 3 can then pass through the heating pipe 32 to heat the flue gas entering through the flue gas inlet 6 . When the temperature of the denitration bed layer 4 is lower than the denitration catalytic activation temperature, the second valve 30 and the third valve 31 are closed, the first valve 29 is opened, and the circulating fluid flows out from the liquid storage tank 14 through the output pump 25, and then passes through the heat exchange Inlet 8, circulation pipeline 13, split grid tube 16, coiled tube 15 in the decarburization bed 3, coiled tube 15 in the third denitrification bed 4, disc in the fourth denitrification bed 4 After the circular tube 15 and the second heat exchange outlet 35, it flows back to the liquid storage tank 14 to complete the cycle. After the circulating fluid absorbs the heat of the decarburization bed 3, when it flows through the coiled tube 15 in the denitrification bed 4, it can The denitrification bed layer 4 is heated. When neither the flue gas entering through the flue gas inlet 6 nor the catalyst of the denitrification bed 4 needs to be heated and kept warm, the first valve 29 and the second valve 30 are closed, the third valve 31 is opened, and the circulating fluid is passed through the liquid storage tank 14 The output pump 25 flows out, passes through the heat exchange inlet 8, the circulation pipeline 13, the split grid pipe 16, the coiled pipe 15 in the decarburization bed 3 and the first heat exchange outlet 9, and then flows back to the storage tank through the return pipe 33. The liquid tank 14 completes the circulation, and the circulating liquid flows back to the liquid storage tank 14 through the return pipe 33 after absorbing the heat of the decarburization bed 3 for storage.

In this embodiment, when the first temperature device 20 detects that the temperature of the decarburization bed 3 is high and has exceeded 180° C., the first temperature device 20 automatically controls the first valve 29, the second valve 30 and the third valve. The valve 31 allows the circulating fluid to flow into the denitrification bed 4 below the decarburization and denitrification tower 1, so that the temperature of the denitrification bed 4 reaches the temperature required for denitrification, so as to meet the normal denitrification. If the first gas detection port 17 and the second gas detection port 28 detect that the _NOx concentration at the outlet of the decarbonization and denitrification tower 1 is relatively high, it means that the denitrification efficiency is low, and the flow direction of the circulating liquid can be manually controlled to make the circulation The liquid flows into the denitrification bed layer 4 to increase the temperature of the denitrification bed layer 4 and ultimately improve the denitrification efficiency.

In this embodiment, both denitrification and decarburization can be realized in a decarbonization and denitrification tower 1, and the heat generated during the decarbonization process can also be fully utilized by means of circulating fluid, that is to say, waste heat can be realized Utilize, the heat that will be used can be used to heat the imported flue gas or supply heat to the denitrification bed layer 4. When neither of these heat is needed, the recovered heat can be used for backup or for other heating equipment. heating.

Example 2:

In this embodiment, as shown in Figure 5, the temperature of the flue gas at the 6 flue gas inlets is 180°C to 240°C, and the sequence of decarbonization and denitrification of the flue gas in the decarbonization and denitrification tower 1 is denitrification first and then decarburization. From the flue gas inlet 6 to the flue gas outlet 7, there are two denitration beds 4 and four decarbonization beds 3 in sequence. The decarburization bed 3 is filled with a catalyst specially used for decarbonization, and the denitrification bed 4 is filled with a special denitrification bed. catalyst. There are two split grid tubes 16, and the two split grid tubes 16 are respectively set upstream of the first decarburization bed 3 and upstream of the second decarburization bed 3. The atomizing nozzle 12 of the ammonia injection equipment is arranged upstream of the first denitrification bed 4 . One temperature detection point 19 is provided, and the temperature detection point 19 is disposed between the second denitrification bed 4 and the first decarburization bed 3 , and the temperature detection point 19 is connected with a first temperature device 20 . The bottoms of the first decarburization bed 3 , the second decarburization bed 3 and the third decarburization bed 3 are all provided with coiled tubes 15 , and the coiled tubes 15 in the decarburization bed 3 and the splitter grid Tube 16 is used to absorb waste heat generated during decarburization. Since the denitrification bed 4 is close to the flue gas inlet 6, the temperature of the flue gas can ensure the denitrification of the denitrification bed 4 normally, and there is no need to provide heat for the catalyst material in the denitrification bed 4. Therefore, no coil pipe is arranged in the denitrification bed 4. 15. The heat released by the oxidation of the three decarburization beds 3 above the fourth decarburization bed 3, after the circulating fluid recovers most of the heat, the remaining heat can raise the temperature of the flue gas to a certain extent, when the flue gas reaches the first When there are four decarburization beds 3, the temperature is sufficient for normal decarburization, and the fourth decarburization bed 3 is at the bottom of the decarburization and denitrification tower 1, considering that a large amount of heat may not be released, so the first The four decarburization bed layers 3 neither utilize waste heat nor supplement heat, so the fourth decarburization bed layer 3 is not provided with a coiled pipe 15 .

In this embodiment, the circulating fluid has only one flow direction, and the circulating fluid flows out from the liquid storage tank 14 through the output pump 25, and then passes through the heat exchange inlet 8, the circulating pipeline 13, the split grid tube 16, and the decarburization bed 3 in sequence. After the coiled tube 15 and the first heat exchange outlet 9, it directly flows back to the liquid storage tank 14, and the heat absorbed by the circulating fluid in the decarburization bed 3 is stored in the liquid storage tank 14. When the first temperature device 20 monitored the temperature of the denitrification bed 4 and the first gas detection port 17 and the second gas detection port 28 detected the concentration value of NO _x to meet the NO _x removal efficiency, the heat of the decarburization bed 3 was determined by After the circulating liquid is collected, it will flow back to the liquid storage tank 14 for standby or provide heat for other equipment that needs heat supply, and there is no need to supply heat for the imported flue gas and the denitrification bed 4 .

Example 3:

In this embodiment, as shown in Figure 6, the temperature of the flue gas at the 6 flue gas inlets is 240°C to 280°C, and the sequence of decarbonization and denitrification of the flue gas in the decarbonization and denitrification tower 1 is simultaneous decarbonization and denitrification. From the gas inlet 6 to the flue gas outlet 7, there are six denitrification and decarbonization beds 5 in sequence. The decarburization catalyst and denitration catalyst in the denitration and decarbonization bed 5 can be the same catalyst or different types of catalysts, depending on the actual situation. Depending on the application situation, the ultimate goal is to simultaneously achieve decarbonization and denitrification. There are two split grid tubes 16, and the two split grid tubes 16 are respectively set upstream of the first denitration and decarburization bed 5 and upstream of the second denitration and decarbonization bed 5. The ammonia injection equipment is set upstream of the first denitrification and decarbonization bed 5. One temperature detection point 19 is provided, and the temperature detection point 19 is disposed upstream of the first denitrification and decarburization bed 5 , and the temperature detection point 19 is connected with a first temperature device 20 . The bottoms of the first denitrification and decarbonization bed 5, the second denitration and decarbonization bed 5 and the third denitration and decarbonization bed 5 are all provided with coiled tubes 15, and the coiled tubes 15 in the denitrification and decarburization bed 5 And the split grid pipe 16 is used to absorb the waste heat generated in the process of decarburization.

In this embodiment, the circulating fluid has only one flow direction, and the circulating fluid flows out from the liquid storage tank 14 through the output pump 25, and then passes through the heat exchange inlet 8, the circulating pipeline 13, the split grid tube 16, and the denitrification and decarburization bed 5 After the inner coiled tube 15 and the first heat exchange outlet 9 , it directly flows back to the liquid storage tank 14 , and the heat absorbed by the circulating fluid in the denitrification and decarburization bed 5 is stored in the liquid storage tank 14 . Since the denitrification and decarburization bed 5 is oxidized in large quantities during decarburization, the temperature of the denitrification and decarburization bed 5 rises, so that the temperature measured by the first temperature device 20 is higher than the temperature required for the denitrification of the denitrification and decarburization bed 5, and the second The first gas detection port 17 and the second gas detection port 28 detect the _NOx concentration at the outlet of the tower body is relatively high, and the denitrification efficiency is low. The temperature of the denitrification and decarburization bed 5 should be lowered by circulating liquid to meet the requirements of simultaneous decarburization and denitrification. temperature requirements.

From the above description, it can be seen that the above-mentioned embodiments of the present invention have achieved the following technical effects:

A device for synchronous decarbonization and denitrification of industrial flue gas and waste heat recovery and utilization. The device can simultaneously decarbonize and denitrify industrial flue gas, and can recycle waste heat generated in the decarbonization process.

Compared with the prior art, the technical solution of the present invention can dynamically adjust the layout of the decarbonization and denitrification tower 1 according to the temperature of the flue gas, and simultaneously perform decarburization and denitrification in the decarbonization and denitrification tower 1, which can greatly save step-by-step processing Equipment investment and reduce floor space, saving costs and operating costs. The present invention effectively recovers the excess heat generated by decarbonization, realizes the resource utilization of waste heat, effectively guarantees the normal operation of denitrification, and at the same time, the recovered heat can also be used for the recovery of the flue gas entering through the flue gas inlet 6 Heating or heat preservation reduces the investment in flue gas heating equipment and keeps the temperature of imported flue gas stable, which is beneficial to decarbonization. The technical solution of the invention can not only decarbonize and denitrify synchronously, but also use waste heat for other purposes according to actual conditions, thereby achieving double benefit effects.

The above descriptions are only preferred embodiments of the present invention, and are not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and changes. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principles of the present invention shall be included within the protection scope of the present invention.

Claims (6)

1. A device for synchronously decarbonizing, denitrating and recycling waste heat of industrial flue gas, which is characterized in that,

the device comprises: a decarbonization and denitration tower, an ammonia spraying device and a reaction bed layer, wherein,

the decarbonization and denitration tower is provided with a flue gas inlet and a flue gas outlet, a plurality of reaction beds are arranged in the decarbonization and denitration tower, the reaction beds are all positioned between the flue gas inlet and the flue gas outlet,

the side wall of the decarburization denitration tower is provided with a heat exchange inlet and a first heat exchange outlet,

an ammonia water inlet is formed in the side wall of the decarburization denitration tower, the ammonia spraying equipment is arranged in the decarburization denitration tower, and the ammonia water inlet is communicated with the ammonia spraying equipment;

the device also comprises a circulating pipeline and a liquid storage tank, wherein an interlayer is arranged on the tower wall of the decarburization and denitration tower, the circulating pipeline is arranged in the interlayer, two ends of the circulating pipeline are respectively communicated with the liquid storage tank through the heat exchange inlet and the first heat exchange outlet,

the bottom of part of the reaction bed layer is provided with a coil pipe which is directly contacted with the catalyst material filled in the reaction bed layer, all the coil pipes in the decarburization and denitration tower are sequentially communicated through the circulating pipeline,

a plurality of flow distribution grating pipes are arranged in the decarburization denitration tower, and inlets and outlets of the flow distribution grating pipes are communicated with the circulation pipeline;

a first gas detection port is formed in the side wall of the decarburization and denitration tower, a first gas detection device is connected with the first gas detection port, a plurality of temperature detection points are arranged in the decarburization and denitration tower, and the temperature detection points are connected with a first temperature device arranged outside the decarburization and denitration tower;

the flue gas inlet is positioned at the top of the decarburization denitration tower, a flue gas pipeline is connected with the flue gas inlet, the flue gas outlet is positioned at the bottom of the decarburization denitration tower, the flue gas outlet is communicated with a discharge pipe, flue gas enters the decarburization denitration tower from the flue gas inlet and is discharged from the flue gas outlet through the discharge pipe, a second temperature device and a second gas detection port are arranged on the discharge pipe, and a second gas detection device is connected with the second gas detection port;

the temperature of the flue gas at the flue gas inlet is 100-180 ℃, the reaction bed layer comprises decarburization beds and denitration beds, a plurality of decarburization beds and a plurality of denitration beds are sequentially arranged from the flue gas inlet to the flue gas outlet, the heat exchange inlet is arranged at the upstream of the first decarburization bed, the ammonia spraying equipment is arranged at the upstream of the first denitration bed, a plurality of flow distribution grid pipes are respectively arranged at the upstream of the plurality of decarburization beds from top to bottom, a second heat exchange outlet is arranged on the side wall of the decarburization denitration tower between the plurality of decarburization beds and the plurality of denitration beds, the circulating pipeline is communicated with the second heat exchange outlet, the second heat exchange outlet is communicated with a heating pipe and a return pipe, the return pipe is communicated with the liquid storage tank, the heating pipe passes through the flue gas pipeline, and the heating pipe is used for heating the flue gas entering the flue gas inlet;

if the temperature of the flue gas at the flue gas inlet is 180-240 ℃, the reaction bed layer comprises a decarburization bed layer and a denitrification bed layer, a plurality of denitrification bed layers and a plurality of decarburization bed layers are sequentially arranged from the flue gas inlet to the flue gas outlet, the heat exchange inlet is arranged at the upstream of the first decarburization bed layer, the ammonia spraying equipment is arranged at the upstream of the first denitrification bed layer, a plurality of flow dividing grating pipes are respectively arranged at the upstream of the plurality of decarburization bed layers from top to bottom,

if the temperature of the flue gas at the flue gas inlet is 240-280 ℃, the reaction bed layer comprises a denitration and decarburization bed layer, a plurality of denitration and decarburization bed layers are sequentially arranged from the flue gas inlet to the flue gas outlet, the heat exchange inlet is arranged at the upstream of the first denitration and decarburization bed layer, the ammonia injection equipment is arranged at the upstream of the first denitration and decarburization bed layer, and the plurality of flow distribution grid pipes are respectively arranged at the upstream of the plurality of denitration and decarburization bed layers from top to bottom.

2. The device for synchronously decarbonizing and denitrating industrial flue gas and recycling waste heat according to claim 1, is characterized in that,

and the interlayer is filled with a heat insulation material.

3. The device for synchronously decarbonizing and denitrating industrial flue gas and recycling waste heat according to claim 1, is characterized in that,

a liquid level meter is arranged on the side wall of the liquid storage tank,

the top end of the liquid storage tank is provided with a liquid injection port and a pressure relief port,

a liquid discharge valve is arranged at the bottom end of the liquid storage tank,

an output pump is arranged on a pipeline between the liquid storage tank and the heat exchange inlet.

4. The device for synchronous decarbonization and denitration and waste heat recovery of industrial flue gas according to claim 1, which is characterized in that,

the ammonia spraying equipment comprises an ammonia water pipeline and an atomizing nozzle, the ammonia water pipeline is used for communicating the ammonia water inlet with the atomizing nozzle,

the first heat exchange outlet is arranged at the downstream of all the reaction beds.

5. The device for synchronously decarbonizing and denitrating industrial flue gas and recycling waste heat according to claim 1, is characterized in that,

carbon means CO and nitro means NO _X The concentration of CO in the flue gas entering the decarburization and denitration tower from the flue gas inlet is 0-15000 mg/Nm ³ 、NO _X The concentration is 0-1000 mg/Nm ³ And the catalyst materials in the reaction bed layer are all formed catalysts.

6. The device for synchronous decarbonization and denitration and waste heat recovery of industrial flue gas according to claim 1, which is characterized in that,

the device also comprises a two-way valve, when a plurality of decarburization beds and a plurality of denitration beds are sequentially arranged in the decarburization denitration tower from the flue gas inlet to the flue gas outlet, the number of the two-way valve is three, the three two-way valve is respectively a first valve, a second valve and a third valve, the first valve is arranged on the circulation pipeline between the denitration beds and the decarburization beds, the second valve is arranged on the heating pipe, the third valve is arranged on the return pipe,

when the flue gas entering from the flue gas inlet needs to be heated and insulated, the first valve and the third valve are closed, the second valve is opened, the circulating liquid can heat the flue gas in the flue gas pipeline through the heating pipe after absorbing the heat of the decarburization bed layer,

when the temperature of the denitration bed layer is lower than the denitration catalytic activation temperature, the second valve and the third valve are closed, the first valve is opened, the denitration bed layer can be heated after the heat of the denitration bed layer is absorbed by the circulating liquid,

when the flue gas entering from the flue gas inlet and the catalyst of the denitration bed layer do not need heating and heat preservation, the first valve and the second valve are closed, the third valve is opened, and circulating liquid flows back to the liquid storage tank through the return pipe after absorbing the heat of the denitration bed layer.

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