Modularized flue gas denitration, heat energy recovery and nitrogen oxide recovery device

Abstract

The utility model relates to the technical field of waste gas treatment, in particular to a modularized flue gas denitration, heat energy recovery and nitrogen oxide recovery device, which comprises a shunting bin, a heat exchanger, a heat exchanger, a nitrogen oxide recovery device and a nitrogen oxide recovery device, and is characterized in that the shunting bin is provided with an inlet and a shunting port along the flowing direction of flue gas; the denitration bin is connected with the flow dividing opening and comprises an adsorption material arranged in the denitration bin in a filling mode, and flue gas directionally flows through the denitration bin in the direction of flowing through the adsorption material; and the flow velocity of the flue gas at the inlet is greater than that of the flue gas at the shunting port. According to the utility model, the shunting bin and the denitration bin are matched with each other, the porous adsorption material is used for reciprocating adsorption and desorption in the denitration bin, the adsorption efficiency is improved through shunting and speed reduction of the shunting bin, ammonia and a catalyst are not required to participate in the process, NOX which is originally required to be converted into N2 is enriched and recycled, and the NOx emission is reduced. And meanwhile, a large amount of original waste heat of the flue gas is recycled, and new value is created.

Description

Technical Field

[0001] The utility model relates to the technical field of waste gas treatment, in particular to a modular flue gas denitration and heat energy recovery and nitrogen oxide recovery device. Background Art

[0002] Denitrification technology is a rigid demand link in the global power generation, metallurgy, building materials, coking, chemical and other industries. SCR denitrification (Selective Catalytic Reduction, referred to as SCR) is a selective catalytic reduction denitrification technology, which has been used for many years as an engineering technology for simultaneous denitrification during flue gas emission. The SCR system uses a catalyst to inject ammonia or other suitable reducing agents into the flue gas to reduce NO in the flue gas at the high temperature section of the flue gas. X Converted into nitrogen and water to complete the denitrification process. Some problems have also been exposed during years of use:

[0003] (1) The operating temperature range is 200-260 degrees Celsius, and the heat energy loss is large;

[0004] (2) Some unreacted NH3 in the system is discharged along with the flue gas, causing secondary air pollution;

[0005] (3) When the flue gas temperature is lower than the catalyst operating temperature range, the reaction efficiency is low, causing the flue gas nitrogen oxides to exceed the standard. Utility Model Content

[0006] The purpose of this section is to summarize some aspects of the embodiments of the utility model and briefly introduce some preferred embodiments. Some simplifications or omissions may be made in this section and the specification abstract and utility model name of this application to avoid blurring the purpose of this section, specification abstract and utility model name, and such simplifications or omissions cannot be used to limit the scope of the utility model.

[0007] In view of the problems existing in the SCR system denitration process in the above-mentioned prior art, the present utility model is proposed.

[0008] Therefore, one of the objects of the present invention is to provide a modular flue gas denitrification and heat recovery and nitrogen oxide recovery device.

[0009] In order to solve the technical problem, the utility model provides the following technical solution: a modular flue gas denitrification and heat recovery and nitrogen oxide recovery device, comprising:

[0010] A diversion chamber is provided with an inlet and a diversion port according to the direction of smoke flow; and

[0011] A denitration chamber, the denitration chamber is connected to the diversion port, and includes an adsorption material filled inside, and the flue gas flows through the denitration chamber in a direction passing through the adsorption material;

[0012] Wherein, the flow rate of the smoke at the inlet is greater than the flow rate of the smoke at the diversion port.

[0013] As a preferred solution of the modular flue gas denitration and heat recovery and nitrogen oxide recovery device of the utility model, wherein: the number of the denitration bins and the diversion ports is the same and no less than two groups, and each group of the denitration bins is connected to the diversion ports in a one-to-one correspondence;

[0014] The sum of the flow cross-sectional areas of the flow outlets of each group is greater than the flow cross-sectional area at the inlet.

[0015] As a preferred solution of the modular flue gas denitration and heat recovery and nitrogen oxide recovery device of the utility model, wherein: the adsorption material in the denitration bin is continuously filled, and the cross-sectional dimensions of the adsorption material in the flue gas flow direction include a transverse dimension and a longitudinal dimension;

[0016] The flue gas flows through the adsorption material in a laminar flow direction of the larger value of the transverse dimension and the longitudinal dimension.

[0017] As a preferred solution of the modular flue gas denitrification and heat recovery and nitrogen oxide recovery device of the utility model, the denitrification bin is provided with an inclined wall adapted to the diversion port, and the flue gas is blocked by the inclined wall and flows through the adsorption material in the direction of the larger value of the transverse dimension and the longitudinal dimension.

[0018] As a preferred solution of the modular flue gas denitration and heat recovery and nitrogen oxide recovery device of the utility model, it also includes a heat exchange device, through which the industrial flue gas forms low-temperature flue gas and hot air or hot water on the exchange side, and the hot water or hot air recovers the heat energy in the flue gas;

[0019] Among them, the low-temperature flue gas flows through the adsorption material, and after the adsorption material is saturated with adsorption, the hot air flows through the adsorption material.

[0020] As a preferred solution of the modular flue gas denitration and heat recovery and nitrogen oxide recovery device of the utility model, one side of the denitration bin is connected to a confluence bin, and the confluence bin is provided with a confluence port and an outlet according to the flue gas flow direction;

[0021] The flue gas passing through the adsorption material flows from the confluence port to the confluence bin.

[0022] As a preferred solution of the modular flue gas denitration and heat recovery and nitrogen oxide recovery device of the utility model, wherein: a plurality of groups of denitration bins are arranged in parallel.

[0023] As a preferred solution of the modular flue gas denitration and heat recovery and nitrogen oxide recovery device of the utility model, wherein: a nitrogen oxide concentration sensor is arranged in the denitration bin, and a control component is connected to the inlet through a pipeline;

[0024] The control assembly includes an air valve for controlling the connection of pipelines, a hot air valve for forming circulating air, and a negative pressure air valve for extracting pressure from the inside to the outside.

[0025] As a preferred solution of the modular flue gas denitrification and heat recovery and nitrogen oxide recovery device of the utility model, the pipeline where the negative pressure air valve is located is connected to a pipeline for transferring the enriched NO X A water washing absorption tower for cooling to generate NO2 and HNO3, wherein the flue gas flows through the water washing absorption tower from bottom to top;

[0026] The water-washing absorption tower is connected to the reaction tower through a pipeline, and the flue gas flowing out of the water-washing absorption tower flows through the reaction tower from bottom to top.

[0027] As a preferred solution of the modular flue gas denitrification and heat recovery and nitrogen oxide recovery device of the utility model, wherein: the reaction towers are arranged in no less than two groups, and the reaction towers in different groups are connected in series in sequence, and the flue gas flowing out of the adjacent groups of reaction towers flows from bottom to top to the next group of reaction towers.

[0028] As a preferred solution of the modular flue gas denitration and heat recovery and nitrogen oxide recovery device of the utility model, wherein: a first absorption liquid buffer pool is provided at the bottom of the water washing absorption tower, and a second absorption liquid buffer pool is provided at the bottom of the reaction tower;

[0029] Wherein, a temporary storage tank is connected between the first absorption liquid buffer tank and the second absorption liquid buffer tank via a pipeline, and a reaction liquid tank is connected between the second absorption liquid buffer tank via a pipeline.

[0030] The utility model is a modular flue gas denitrification and heat recovery and nitrogen oxide recovery device with beneficial effects: the utility model cooperates with the diversion chamber and the denitrification chamber, uses porous adsorption materials to reciprocate adsorption and desorption in the denitrification chamber, and improves the adsorption efficiency by diversion and deceleration of the diversion chamber. No ammonia and catalyst are required in the process, and NO that originally needs to be converted into N2 X It not only enriches and recycles the flue gas, but also recycles a large amount of waste heat from the flue gas, creating new value. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] In order to more clearly illustrate the technical solutions of the embodiments of the present utility model, the following briefly introduces the drawings required for the description of the embodiments. Obviously, the drawings described below are only some embodiments of the present utility model. For ordinary technicians in this field, other drawings can be obtained based on these drawings without creative labor. Among them:

[0032] Figure 1 This is a schematic diagram of the structure of Example 1 of the utility model.

[0033] Figure 2 This is a schematic diagram of the structure in Example 2 of the utility model.

[0034] Figure 3 This is a schematic diagram of the structure in Example 3 of the utility model.

[0035] Figure 4 This is a schematic diagram of the structure in Example 4 of the utility model.

[0036] Figure 5 This is a schematic diagram of the connection between the heat exchange device and the denitrification bin in Example 5 of the utility model.

[0037] Figure 6 This is a schematic diagram of the structure of the heat exchange device in Example 5 of the utility model.

[0038] Figure 7 This is a schematic diagram of the structure in Example 6 of the utility model.

[0039] Figure 8 This is a schematic diagram of the structure in Example 7 of the utility model.

[0040] Fig. 9 It is a schematic diagram of the composition principle of each module of the utility model. DETAILED DESCRIPTION

[0041] In order to make the objectives, features and advantages of the present invention more obvious and understandable, the specific implementation methods of the present invention are described in detail below in conjunction with the accompanying drawings.

[0042] In the following description, many specific details are set forth to facilitate a full understanding of the present invention, but the present invention may also be implemented in other ways different from those described herein, and those skilled in the art may make similar generalizations without violating the connotation of the present invention. Therefore, the present invention is not limited to the specific embodiments disclosed below.

[0043] Secondly, the term "one embodiment" or "embodiment" as used herein refers to a specific feature, structure or characteristic that may be included in at least one implementation of the present invention. The term "in one embodiment" that appears in different places in this specification does not necessarily refer to the same embodiment, nor does it refer to a separate or selective embodiment that is mutually exclusive with other embodiments.

[0044] Example 1

[0045] Reference Figure 1 , which is the first embodiment of the utility model, and provides a modular flue gas denitrification and heat recovery and nitrogen oxide recovery device, which mainly includes: a diversion chamber 200 and a denitrification chamber 100, and the diversion chamber 200 is used to reduce the speed of the flowing flue gas to improve the adsorption efficiency of the flue gas after entering the denitrification chamber 100, and the adsorption material in the denitrification chamber 100 is used to adsorb the nitrogen oxides in the flue gas.

[0046] Specifically, the diversion chamber 200 is a connecting passage connected to the outside of the denitrification chamber 100, and is provided with an inlet 201 and a diversion port 202 according to the flow direction of the flue gas. The flue gas enters the diversion chamber 200 from the inlet 201 at a high flow rate, and after being decelerated in the diversion chamber 200, it enters the denitrification chamber 100 through the diversion port 202 at a low flow rate.

[0047] Furthermore, the denitration bin 100 is filled with an adsorption material C1. The adsorption material C1 selected in this embodiment is a rigid porous sphere or a rigid porous cylinder. The diameter of the sphere is between 0.3 and 10 mm, and the diameter of the cylinder is between 1 and 12 mm. The surface is a porous structure with a pore size of 1 to 20 μm, a porosity of 50 to 90%, and a BET specific surface area of ​​400 m 2 / g, BET specific surface area refers to the total area per unit mass of the material. Among them, micropores and mesopores are mainly distributed on the surface of the sphere, which can facilitate the rapid adsorption and desorption of NO X gas.

[0048] The rigid porous beads of the adsorption material C1 can be spherical, cylindrical or spheroidal, which are generated by calcining and compounding carbon-based materials, metal salts and polymer materials, and have porous physical properties; at the same time, different pore opening agents can generate the required pore size. The metal generated by high-temperature calcination and reduction of metal salts is selected as the framework, and the porous adsorption medium needs to have high strength, high temperature resistance, good wear resistance, and no powder shedding. Optional polymer materials or aluminum oxide, zinc oxide, manganese oxide, silicon dioxide, aluminum silicate, diatomaceous earth, graphite, activated coke, activated carbon, carbon fiber, carbon nanotubes, titanium dioxide, silicon carbide, silicon nitride, rare earth materials, or mixtures thereof. Preferred are aluminum oxide, aluminum silicate, silicon dioxide, manganese oxide, carbon-based materials, and nitrogen-containing polymer materials.

[0049] It should be noted that the number of diversion ports 202 is determined by the number of denitration bins 100, and only one group may be provided, or different denitration bins 100 may be connected through multiple groups of diversion ports 202. In this embodiment, the denitration bins 100 are provided in multiple groups, so that under the condition of achieving the same denitration efficiency, the amount of adsorption material C1 filled in the denitration bins 100 in a single group can be less, which is convenient for replacement and maintenance.

[0050] Among them, in order to ensure that the flow rate of the flue gas at the inlet 201 of the diversion chamber 200 is greater than the flow rate of the flue gas at the diversion port 202, a diversion pressure regulation and speed reduction control flow rate can be adopted, such as setting a baffle with an aperture or a gap between the inlet 201 and the diversion port 202, and regulating the pressure of the fluid to control the flow rate through the baffle. In this embodiment, the diversion chamber 200 is composed of pipelines, wherein the inlet 201 is a main pipeline, and the main pipeline is connected to each group of denitrification chambers 100 through branch pipelines, and the connection between the branch pipeline and the denitrification chamber 100 is the diversion port 202. After the flue gas enters the diversion chamber 200 from the inlet 201 of the main pipeline, it will disperse and flow into each group of branch pipelines to achieve speed reduction laminar flow. Preferably, the branch pipeline and the main pipeline are non-parallel, that is, after the flue gas enters the branch pipeline from the main pipeline of the inlet 201, the inner wall of the branch pipeline also has a blocking and speed reduction effect on the flowing flue gas.

[0051] Example 2

[0052] Reference Figure 2 , which is the second embodiment of the present utility model. Different from the previous embodiment, in this embodiment, the sum of the flow cross-sectional areas of the flow outlets 202 of each group is set to be larger than the flow cross-sectional area at the inlet 201.

[0053] The flow rate L of a fluid passing through a certain point in a unit time can be expressed by the flow cross-sectional area S and the flow velocity V, that is, L = SV (Formula 1). In order to maintain the pressure balance in the diversion chamber (200), the amount of smoke L flowing in from the inlet 201 per unit time is 入 The total amount of flue gas L flowing out of the diversion port 202 出 equal.

[0054] Among them, L 入 =S 入 V 入 (Formula 2), in this formula, S 入 is the flow cross-sectional area at the inlet 201, V 入 is the flue gas velocity at the inlet 201. 出 =S1V1+S2V2+...S i V i +...+S n V n (Formula 3), in which n represents a total of n groups of flow ports 202, S i is the flow cross-sectional area at any branch port 202, Vi is the flue gas velocity at any branch outlet 202, and the total amount of flue gas flowing out of the branch outlet 202 is L 出 It is the sum of the flue gas flow rates at each branch outlet (202).

[0055] In this embodiment, the flow cross-sectional area S at each branch port 202 is i The size of is set to be the same, so that the flue gas flow velocity V at each branch port 202 i Approximately equal, so L 出 =(S1+S2+...S i +...+S n )*V i (Formula 4), when L 入 =L 出 , and requires V 入 >V i , the total cross-sectional area of ​​each branch port (202) should be S 出 >S 入 , we get formula 5:

[0056] Therefore, the flow cross-sectional area S of each group of flow ports 202 can also be adjusted. i The flow cross-sectional area S at the inlet 201 入 In this embodiment, the diversion chamber 200 is preferably a common chamber structure, with only gaps at the inlet 201 and the diversion port 202 to allow smoke to flow, and the rest of the structure is a closed structure, which can save many pipeline connections and save costs.

[0057] Example 3

[0058] Reference Figure 3 , which is the third embodiment of the utility model. Different from the previous embodiment, in this embodiment, the smoke flows through the adsorption material C1 in the direction of the larger value of the transverse dimension D1 and the longitudinal dimension D2.

[0059] Specifically, the adsorption material C1 in the denitration bin 100 is continuously filled, that is, the adsorption material C1 is a whole without obvious segmentation, and the adsorption material C1 can usually be shaped and filled by a mesh structure, etc. The cross-sectional dimensions of the adsorption material C1 in the flue gas flow direction include a transverse dimension D1 and a longitudinal dimension D2. The cross-sectional dimension of the adsorption material C1 in the flue gas flow direction is the cross-sectional dimension of the plane parallel to the flue gas flow direction. The thickness dimension of the cross-sectional dimension is adapted to the time required for the flue gas to pass through. The thicker the cross-sectional dimension, the longer the time required for the flue gas to pass through the adsorption material C1.

[0060] It should be noted that the transverse dimension D1 and the longitudinal dimension D2 of the adsorption material C1 are relative dimensions, that is, the dimensions measured in two mutually perpendicular directions. The adsorption material C1 can obtain different transverse dimensions D1 and longitudinal dimensions D2 by rotating arbitrarily in the plane. When the smoke passes through the adsorption material C1 from a certain direction, the larger the contact surface with the adsorption material C1, the more smoke will participate in the flow at the same time when the pressure is the same. The greater the depth of the smoke passing through the adsorption material C1 at a certain position, the greater the obstacle encountered in theory, the longer the time required, but the better the adsorption effect.

[0061] Preferably, the flue gas flows through the adsorption material C1 in the direction of the larger value of the transverse dimension D1 and the longitudinal dimension D2. While ensuring that the depth of the flue gas passing through the adsorption material C1 at any position meets the required adsorption effect, the flue gas should be selected to flow through the adsorption material C1 from a direction with a larger contact surface of the adsorption material C1, that is, the direction indicated by the larger value of the transverse dimension D1 and the longitudinal dimension D2 in the adsorption material C1. In this embodiment, the flue gas flow rate in the denitrification bin 100 is reduced to 0.1m / s-0.8m / s, and the flue gas flows through the adsorption material C1 from the direction with the largest contact surface of the adsorption material C1. Preferably, the adsorption material C1 is set to be of equal thickness, so that when the flue gas passes through from the direction with the largest contact surface, the penetration time at each position is kept similar, and the adsorption effect on the flue gas is more uniform.

[0062] Example 4

[0063] Reference Figure 4 , which is the fourth embodiment of the utility model. Different from the previous embodiment, this embodiment provides an inclined wall 101 adapted to the diversion port 202 .

[0064] Specifically, the denitrification chamber 100 is provided with an inclined wall 101 adapted to the diversion port 202, the inclined wall 101 is arranged toward the side where the adsorption material C1 is located, and the inclined wall 101 covers the diversion port 202 in the vertical direction of the figure, so that the flowing flue gas entering from the diversion port 202 will be directly blocked by the inclined wall 101, so that the flue gas can pass through the adsorption material C1 in a laminar flow at an equal pressure, so that the adsorption saturation time is similar; preferably, the inclined wall 101 completely covers the adsorption material C1 in the vertical direction of the figure, so that the flue gas flowing in from the diversion port 202 with a shorter diameter passes through the adsorption material C1 in a laminar flow through the inclined wall 101.

[0065] It is worth noting that, in consideration of energy conservation and consumption reduction and the cost of use, the volume occupied by the diversion bin 200 set on one side of each group of denitrification bins 100 should be reduced as much as possible in practice. After the volume of each group of denitrification bins 100 is determined, the interval between adjacent denitrification bins 100 should be reduced as much as possible, and connected by the side with the larger dimension, so that the diversion bin 200 can be connected with the side with the smaller dimension of each group of denitrification bins 100, thereby reducing the total length of the diversion bin 200. Limited by the size of the denitrification bin 100, the adsorption material C1 inside the denitrification bin 100 should also be adaptively set to achieve better space utilization. In this embodiment, the cross-section of the adsorption material C1 in the direction of flue gas flow is a rectangle, and the short side of the rectangle is set on the side of the diversion port 202 of the denitrification bin 100, which can minimize the interval between adjacent denitrification bins 100.

[0066] Preferably, after being blocked by the inclined wall 101, the flue gas flows through the adsorption material C1 in a laminar flow in the direction where the contact surface of the adsorption material C1 is the largest, so that the adsorption saturation time of the adsorption material C1 is similar, thereby ensuring a stable denitrification effect.

[0067] Example 5

[0068] Reference Figure 5 and Figure 6 , which is the fifth embodiment of the utility model. Different from the previous embodiment, this embodiment further provides a heat exchange device 300.

[0069] Specifically, the industrial flue gas passes through the heat exchange device 300 to form low-temperature flue gas and hot air or hot water. The heat exchange device 300 is a heat exchanger commonly used in the prior art, and its working principle is to exchange heat between cold medium and hot medium. Industrial flue gas generally contains high heat, with a temperature of 240 degrees Celsius to 120 degrees Celsius and a flow rate of 1000m3 / h-1000000m3 / h.

[0070] After the hot flue gas is dedusted by the dust collector, it is passed into the heat exchange device 300 for heat energy recovery. The hot side of the heat exchange device 300 is hot flue gas, and the heat energy is mainly the waste heat contained in the flue gas; the cold side of the heat exchange device 300 is cold water or cold air. For example: after the normal temperature cold water passes through the heat exchange device 300, the flue gas temperature is reduced to 30-70 degrees Celsius, and the cold water temperature is increased to 40-95 degrees Celsius, which can be used as a thermal energy source. In this heat transfer process, the heat energy in the hot flue gas that was originally unrecoverable is recovered, and the recovery efficiency is >80%. At the same time, this process condenses the latent heat saturated water in the industrial flue gas, reducing the impact of saturated water in the flue gas on the atmosphere. In this embodiment, the heat exchange device 300 includes a flue gas-cold water heat exchange group 301, a flue gas-air heat exchange group 302, and a flue gas-cold water heat exchange group 303 connected in sequence, and each heat exchange group is respectively provided with an inlet and an outlet, and 90°C hot water can be obtained by heat exchange of high-temperature flue gas, and the heat energy recovery rate is higher than 80%.

[0071] Among them, the low-temperature flue gas and the hot air flow through the denitrification chamber 100 in a directional manner in the direction of flowing through the adsorption material C1 in sequence. First, after the low-temperature flue gas flows through the adsorption material C1, the nitrogen oxides contained in the flue gas will be adsorbed and retained in the pores of the adsorption material C1; when the nitrogen oxides in the adsorption material C1 are saturated, hot air flows through the adsorption material C1 containing nitrogen oxides, so that the nitrogen oxides are desorbed and enriched with the hot air flow. The nitrogen oxides adsorbed by the adsorption material C1 can be fully desorbed by circulating the hot air flow or hot air containing nitrogen oxides through the adsorption material C1.

[0072] In the above adsorption process, no ammonia is involved, which can solve the secondary pollution problem of flue gas ammonia escape. No catalyst is involved, which avoids the problem that certain pollutants can poison the catalyst when the flue gas composition is complex. Through the reciprocating adsorption and desorption of the adsorption material C1, NO that needs to be converted into N2 can be X Enrichment and recycling, NO X After enrichment, it can react to produce nitric acid or ammonium nitrate, nitrate and other industrial products, creating new value.

[0073] Example 6

[0074] Reference Figure 7 , which is the sixth embodiment of the present utility model. Different from the previous embodiment, this embodiment also includes a confluence bin 400.

[0075] Specifically, one side of the denitrification bin 100 is connected to a confluence bin 400, and the confluence bin 400 is provided with a confluence port 401 and an outlet 402 according to the direction of flue gas flow; flue gas enters the denitrification bin 100 from the diversion port 202, and can flow out of the denitrification bin 100 from the confluence port 401 after passing through the adsorption material C1. The flue gas that flows through the adsorption material C1 flows from the confluence port 401 to the confluence bin 400, and the flue gas that enters the confluence bin 400 from the confluence port 401 eventually flows out through the outlet 402. In this embodiment, the confluence bin 400 is correspondingly arranged with the diversion bin 200, that is, after the airflow entering the denitrification bin 100 is reversed, the corresponding positions and functions of the confluence bin 400 and the diversion bin 200 will be replaced accordingly without affecting the operation (the same below).

[0076] Furthermore, a nitrogen oxide concentration sensor 500 is provided in the denitration chamber 100 (the nitrogen oxide concentration sensor 500 is a prior art, and the specific structure is not shown in the attached drawings). The real-time nitrogen oxide gas concentration in the denitration chamber 100 can be measured by the nitrogen oxide concentration sensor 500. Due to the interconnected state, the nitrogen oxide concentration sensor 500 can also be installed in the diversion chamber 200 or the confluence chamber 400. The inlet 201 and the outlet 402 are both connected to the control component 600 through a pipeline, and the fluid in and out is controlled by the control component 600, which is convenient for overall control and regulation; in this embodiment, the inlet 201 and the outlet 402 are both determined relative to the flow direction of the airflow. When the airflow enters from the outlet 402 side in the opposite direction, the corresponding positions and functions of the inlet 201 and the outlet 402 will be replaced accordingly without affecting the operation (the same below).

[0077] The control component 600 includes an air valve 601 for controlling the connection of the pipeline, a hot air valve 602 for forming circulating air, and a negative pressure air valve 603 for extracting pressure from the inside to the outside. In this embodiment, pipelines are connected to the inlet 201 and the outlet 402. Among them, the pipeline connected by the air valve 601 controls the outflow of low-temperature flue gas and waste gas after adsorption, the pipeline connected by the hot air valve 602 controls the inflow and outflow of hot air and desorbed hot air, and the negative pressure air valve 603 discharges the air flow inside the device.

[0078] Adsorption process: First, the air valve 601 on the inlet 201 side and the outlet 402 side is opened, and the hot air valve 602 and the negative pressure air valve 603 are closed, so that the low-temperature flue gas cooled by the heat exchange device 300 enters the denitration chamber 100 through the inlet 201 and flows through the adsorption material C1, wherein the nitrogen oxides in the flue gas are adsorbed by the adsorption material C1, and the denitrated flue gas is discharged through the outlet 402;

[0079] Desorption process: when the adsorption material C1 in the denitration bin 100 is saturated with adsorption, the air valves 601 on the inlet 201 side and the outlet 402 side are closed, and the hot air valves 602 on both sides are opened, and the heated hot air enters the denitration bin 100 through the inlet 201 to desorb the nitrogen oxides adsorbed in the adsorption material C1. After the desorbed nitrogen oxides flow is removed from the outlet 402, it can be re-connected to the denitration bin 100 through the hot air valve 602 on the other side, and the adsorption material C1 is continuously passed through to increase the nitrogen oxide content in the air flow; it can also be circulated in reverse until the nitrogen oxide concentration sensor 500 installed in the denitration bin 100 measures that the nitrogen oxide concentration of the gas in the bin reaches the set value, and the hot air valves 602 on both sides are closed, and then the negative pressure air valve 603 is opened to extract the nitrogen oxide-containing gas in the bin and send it to the subsequent multi-stage absorption tower. This process is repeated many times until the adsorption material C1 completely desorbs the nitrogen oxides, and the process is stopped. The chamber can then be cooled, which can be air-cooled or liquid-cooled, to reach a preparatory state at room temperature.

[0080] Example 7

[0081] Reference Figure 8 and Fig. 9 , which is the seventh embodiment of the present utility model. Different from the previous embodiment, this embodiment further provides a water washing absorption tower 700 and a reaction tower 800.

[0082] Specifically, the pipeline where the negative pressure air valve 603 is located is connected to a pipeline for transferring the enriched NO X The water washing absorption tower 700 generates HNO3, and the flue gas flows through the water washing absorption tower 700 from bottom to top. The water washing absorption tower 700 enriches NO X By simultaneously adding oxygen or oxygen-containing oxides, such as H2O2, O3, etc.; the water washing absorption tower 700 adopts a common tower structure. After the adsorption and desorption process, the flue gas containing nitrogen oxides flows from bottom to top through the water washing absorption tower 700 and is cooled by pure water. Nitrogen dioxide is absorbed by water and reacts to generate nitric acid. The main purpose is to cool the flue gas and control the outlet gas flow temperature at 20-30°C. Since the main components of the flue gas are NO and the content of O2 is low, the amount converted to NO2 is also low, so the concentration of HNO3 in the absorption liquid is low at this time.

[0083] Specifically, the water washing absorption tower 700 is connected to the reaction tower 800 through a pipeline, and the flue gas flowing out of the water washing absorption tower 700 flows through the reaction tower 800 from bottom to top; the reaction tower 800 is also a tower structure, and the reaction liquid is used to react and remove the nitrogen dioxide and nitric acid in the cooled flue gas. In this process, sufficient air required for the reaction can also be supplemented according to the amount of incoming gas.

[0084] Furthermore, at least two groups of reaction towers 800 are provided, and different groups of reaction towers 800 are connected in series in order, and the flue gas flowing out of the adjacent groups of reaction towers 800 flows from bottom to top to the next group of reaction towers 800; the reaction towers 800 store liquids that react with NO2 and HNO3 (for example: ammonia water, hydroxide ion liquid), which can react with HNO3 to generate ammonium nitrate liquid and nitrate ion liquid. By setting multiple groups of reaction towers 800 in series, the flue gas that is not completely absorbed in the previous group of reaction towers 800 can be absorbed again, and generally two groups of reaction towers 800 can meet the needs. The remaining gas can be extracted from the top of the last group of reaction towers 800 by a centrifugal fan.

[0085] Preferably, a first absorption liquid buffer pool 701 is provided at the bottom of the water-washing absorption tower 700, and a second absorption liquid buffer pool 801 is provided at the bottom of the reaction tower 800; a temporary storage pool 702 is connected between the first absorption liquid buffer pool 701 and the second absorption liquid buffer pool 801 through a pipeline, and a reaction liquid pool 802 is connected between the second absorption liquid buffer pool 801 through a pipeline. By providing the first absorption liquid buffer pool 701 and the second absorption liquid buffer pool 801, the absorption liquid can be stored, and the first absorption liquid buffer pool 701 and the second absorption liquid buffer pool 801 can be connected to the corresponding absorption tower through a circulating water pump. By providing the temporary storage pool 702, the reaction liquid with lower purity can be stored for convenient recirculation and absorption; the reaction liquid pool 802 can store the reaction liquid with higher concentration, and the temporary storage pool 702 and the reaction liquid pool 802 can be provided with concentration probes to facilitate the control of the internal liquid concentration. Preferably, magnetic flap level gauges may be provided in the first absorption liquid buffer tank 701 and the second absorption liquid buffer tank 801 to facilitate control of the liquid level and to pump and drain the internal absorption liquid according to the liquid level.

[0086] Importantly, it should be noted that the construction and arrangement of the present application shown in a plurality of different exemplary embodiments are only exemplary. Although only a few embodiments are described in detail in this disclosure, it should be readily understood by those who refer to this disclosure that many modifications are possible (e.g., the size, scale, structure, shape and ratio of various elements, and parameter values ​​(e.g., temperature, pressure, etc.), installation arrangements, use of materials, color, directional changes, etc.) without substantially departing from the novel teachings and advantages of the subject matter described in the application. For example, the element shown as integrally formed can be composed of multiple parts or elements, the position of the element can be inverted or otherwise changed, and the nature or number or position of the discrete element can be changed or changed. Therefore, all such modifications are intended to be included in the scope of the present utility model. The order or sequence of any process or method steps can be changed or reordered according to alternative embodiments. In the claims, any "device plus function" clause is intended to cover the structure of performing the function described herein, and is not only structurally equivalent but also equivalent structure. Without departing from the scope of the present invention, other substitutions, modifications, changes and omissions may be made in the design, operating conditions and arrangement of the exemplary embodiments. Therefore, the present invention is not limited to a specific embodiment, but extends to various modifications that still fall within the scope of the appended claims.

[0087] Additionally, in order to provide a concise description of example embodiments, all features of an actual embodiment (ie, those features that are not relevant to the best mode presently contemplated for carrying out the invention or those that are not relevant to implementing the invention) may not be described.

[0088] It will be appreciated that in the development of any actual implementation, as in any engineering or design project, numerous implementation-specific decisions may be made. Such a development effort may be complex and time-consuming, but will be a routine task of design, fabrication, and production for those of ordinary skill having the benefit of this disclosure without undue experimentation.

[0089] It should be noted that the above embodiments are only used to illustrate the technical solution of the utility model rather than to limit it. Although the utility model has been described in detail with reference to the preferred embodiments, ordinary technicians in the field should understand that the technical solution of the utility model can be modified or replaced by equivalents without departing from the spirit and scope of the technical solution of the utility model, which should be included in the scope of the claims of the utility model.

Claims

1. A modular flue gas denitrification and heat recovery and nitrogen oxide recovery device, characterized by: include, A diversion chamber (200), wherein the diversion chamber (200) is provided with an inlet (201) and a diversion port (202) according to the direction in which smoke flows; and A denitration bin (100), the denitration bin (100) being connected to the diversion port (202), comprising an adsorption material (C1) filled inside, and the flue gas directional-flowing through the denitration bin (100) in a direction passing through the adsorption material (C1); Wherein, the flow rate of the smoke at the inlet (201) is greater than the flow rate of the smoke at the diversion port (202); The denitration bins (100) and the diversion ports (202) are provided in the same number and are not less than two groups, and each group of denitration bins (100) is connected to the diversion ports (202) in a one-to-one correspondence; The sum of the flow cross-sectional areas of the flow outlets (202) of each group is greater than the flow cross-sectional area at the inlet (201).

2. The modular flue gas denitrification and heat recovery and nitrogen oxide recovery device according to claim 1 is characterized in that: The adsorption material (C1) in the denitration bin (100) is continuously filled, and the cross-sectional dimensions of the adsorption material (C1) in the flue gas flow direction include a transverse dimension (D1) and a longitudinal dimension (D2); The flue gas flows through the adsorption material (C1) in the direction of the larger value of the transverse dimension (D1) and the longitudinal dimension (D2).

3. The modular flue gas denitrification and heat recovery and nitrogen oxide recovery device according to claim 2 is characterized in that: The denitration bin (100) is provided with an inclined wall (101) adapted to the diversion port (202); after being blocked by the inclined wall (101), the flue gas flows through the adsorption material (C1) in a laminar flow in a direction having a larger value between a transverse dimension (D1) and a longitudinal dimension (D2).

4. The modular flue gas denitrification combined with heat recovery and nitrogen oxide recovery device according to claim 1 or 3, characterized in that: It also includes a heat exchange device (300), through which the industrial flue gas passes through the heat exchange device (300) to form low-temperature flue gas and hot air or hot water on the exchange side, and the hot water or hot air recovers heat energy in the flue gas; The low-temperature flue gas flows through the adsorption material (C1), and after the adsorption material (C1) is saturated with adsorption, the hot air flows through the adsorption material (C1).

5. The modular flue gas denitrification and heat recovery and nitrogen oxide recovery device according to claim 4, characterized in that: One side of the denitration bin (100) is connected to a confluence bin (400), and the confluence bin (400) is provided with a confluence port (401) and an outlet (402) according to the flue gas flow direction; The flue gas that has passed through the adsorption material (C1) flows from the confluence port (401) to the confluence bin (400).

6. The modular flue gas denitrification combined with heat recovery and nitrogen oxide recovery device according to any one of claims 1, 3 and 5, characterized in that: The denitration bins (100) are arranged in multiple groups in parallel.

7. The modular flue gas denitrification and heat recovery and nitrogen oxide recovery device according to claim 6, characterized in that: A nitrogen oxide concentration sensor (500) is provided in the denitration bin (100), and the inlet (201) is connected to a control component (600) via a pipeline; The control component (600) comprises an air valve (601) for controlling the connection of pipelines, a hot air valve (602) for forming circulating air, and a negative pressure air valve (603) for extracting pressure from the inside to the outside.

8. The modular flue gas denitrification and heat recovery and nitrogen oxide recovery device according to claim 7, characterized in that: The pipeline where the negative pressure air valve (603) is located is connected to a pipeline for transferring the enriched NO X A water washing absorption tower (700) for cooling to generate NO2 and HNO3, wherein the flue gas flows from bottom to top through the water washing absorption tower (700); The water-washing absorption tower (700) is connected to the reaction tower (800) via a pipeline, and the flue gas flowing out of the water-washing absorption tower (700) flows through the reaction tower (800) from bottom to top.

9. The modular flue gas denitrification combined with heat recovery and nitrogen oxide recovery device according to claim 8, characterized in that: The reaction towers (800) are arranged in no less than two groups, and the reaction towers (800) of different groups are connected in series in sequence, and the flue gas flowing out of the adjacent groups of reaction towers (800) flows from bottom to top to the next group of reaction towers (800).

10. The modular flue gas denitrification combined with heat recovery and nitrogen oxide recovery device according to claim 9, characterized in that: A first absorption liquid buffer pool (701) is provided at the bottom of the water-wash absorption tower (700), and a second absorption liquid buffer pool (801) is provided at the bottom of the reaction tower (800); The first absorption liquid buffer pool (701) and the second absorption liquid buffer pool (801) are connected to a temporary storage pool (702) via a pipeline, and the second absorption liquid buffer pool (801) is connected to a reaction liquid pool (802) via a pipeline.

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