CN114471108B - Synchronous decarbonization denitration of industry flue gas and waste heat recovery utilize's device - Google Patents
Synchronous decarbonization denitration of industry flue gas and waste heat recovery utilize's device Download PDFInfo
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- CN114471108B CN114471108B CN202210134707.6A CN202210134707A CN114471108B CN 114471108 B CN114471108 B CN 114471108B CN 202210134707 A CN202210134707 A CN 202210134707A CN 114471108 B CN114471108 B CN 114471108B
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- B01D53/34—Chemical or biological purification of waste gases
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- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D1/00—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators
- F28D1/02—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid
- F28D1/04—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid with tubular conduits
- F28D1/047—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid with tubular conduits the conduits being bent, e.g. in a serpentine or zig-zag
- F28D1/0477—Heat-exchange apparatus having stationary conduit assemblies for one heat-exchange medium only, the media being in contact with different sides of the conduit wall, in which the other heat-exchange medium is a large body of fluid, e.g. domestic or motor car radiators with heat-exchange conduits immersed in the body of fluid with tubular conduits the conduits being bent, e.g. in a serpentine or zig-zag the conduits being bent in a serpentine or zig-zag
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
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- B01D2251/2062—Ammonia
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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
Technical Field
The invention relates to the field of industrial flue gas treatment, in particular to a device for synchronous decarbonization and denitration and waste heat recovery of industrial flue gas.
Background
At present, in the industrial production process, a large amount of harmful gas is generated to remove SO 2 In addition, CO and NO X But also seriously pollute the environment and influence the normal life of people.
In view of the diversity of pollutant components in industrial waste gas and the further research and development and application of the multi-pollutant synchronous removal technology, the synchronous decarburization and denitration is receiving extensive attention and research from various circles, wherein the low-temperature denitration process using the catalyst is also becoming more mature, and the related research and application are actively promoted in various places. However, in the same tower body, in the synchronous decarburization and denitration process, due to the fact that the reaction temperature ranges of the two cause the problems of rapid rise of the temperature of a denitration bed layer in the denitration process, excessive oxidation of reducing agent ammonia gas and other practical applications, the denitration activity is finally greatly reduced, and outlet NO is caused X The emission is not up to standard, so the technical requirement of fully recycling redundant heat generated by the decarbonization bed layer in the synchronous decarbonization and denitration process to realize high-efficiency denitration of the denitration bed layer is urgent.
In view of the above, there is a need for an apparatus for synchronous decarbonization and denitration and waste heat recovery of industrial flue gas.
Disclosure of Invention
The invention aims to provide a device for synchronous decarburization and denitration and waste heat recovery of industrial flue gas, which finally realizes the normal operation of synchronous decarburization and denitration of a reaction bed layer by adopting a mode of synchronous decarburization and denitration and waste heat recovery, the reaction bed layers reach respective high removal activity at respective proper operating temperature, and meanwhile, the redundant heat of the decarburization bed layer can also be applied in various aspects.
In order to achieve the above purpose, the invention provides the following technical scheme:
the utility model provides a synchronous decarbonization denitration of industry flue gas and waste heat recovery utilize's device, the device includes: 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.
Further, in the device for synchronous decarbonization, denitration and waste heat recovery of industrial flue gas, a circulation pipeline and a liquid storage tank are further included, an interlayer is arranged on the tower wall of the decarbonization and denitration tower, the circulation pipeline is arranged in the interlayer, two ends of the circulation pipeline are respectively communicated with the liquid storage tank through the heat exchange inlet and the first heat exchange outlet, a coil pipe is arranged at the bottom of part of the reaction bed layer, the coil pipe is in direct contact with the catalyst material filled in the reaction bed layer, all the coil pipes in the decarbonization and denitration tower are sequentially communicated through the circulation pipeline, a plurality of shunt grid pipes are arranged in the decarbonization and denitration tower, and the inlets and outlets of the shunt grid 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; preferably, the interlayer is filled with a heat insulation material.
Further, in foretell synchronous decarbonization denitration of industrial flue gas and waste heat recovery utilize's device, be provided with the level gauge on the lateral wall of liquid reserve tank, the top of liquid reserve tank is provided with annotates liquid mouth and pressure release mouth, the bottom of liquid reserve tank is provided with the flowing back valve the liquid reserve tank with be provided with the delivery pump on the pipeline between the heat transfer import.
Further, in the above apparatus for synchronous decarbonization and denitration of industrial flue gas and recovery and utilization of waste heat, the ammonia injection device includes an ammonia water pipeline and an atomizing nozzle, the ammonia water pipeline is used for communicating the ammonia water inlet with the atomizing nozzle, and the first heat exchange outlet is disposed at the downstream of all the reaction beds.
Further, in the above device for synchronous decarbonization and denitration of industrial flue gas and waste heat recovery, the flue gas inlet is located at the top of the decarbonization and denitration tower, the flue gas pipeline is connected with the flue gas inlet, the flue gas outlet is located at the bottom of the decarbonization and denitration tower, the flue gas outlet is communicated with the discharge pipe, flue gas enters the decarbonization and denitration tower from the flue gas inlet, is discharged from the flue gas outlet through the discharge pipe, the discharge pipe is provided with a second temperature device and a second gas detection port, and the second gas detection port is connected with a second gas detection device.
Further, in the above apparatus for synchronous decarbonization and denitration and waste heat recovery of industrial flue gas, the carbon refers to CO, and the nitrate refers to 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.
Further, in the above device for synchronous decarbonization and denitration of industrial flue gas and waste heat recovery, if the temperature of flue gas at the flue gas inlet is 100-180 ℃, the reaction bed layer includes a decarbonization bed layer and a denitration bed layer, from the flue gas inlet to the flue gas outlet, a plurality of decarbonization bed layers and a plurality of denitration bed layers are sequentially arranged, the heat exchange inlet is arranged at the upstream of the first decarbonization bed layer, the ammonia injection device is arranged at the upstream of the first denitration bed layer, a plurality of grid shunt pipes are respectively arranged at the upstream of the plurality of decarbonization bed layers from top to bottom, a second heat exchange outlet is arranged on the side wall of the decarbonization and denitration tower between the plurality of decarbonization bed layers and the plurality of denitration bed layers, the circulation pipeline is communicated with the second heat exchange outlets, 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 is used for heating the flue gas entering the flue gas inlet.
Further, in the above-mentioned synchronous decarbonization denitration of industrial flue gas and waste heat recovery utilize's device, if the temperature of flue gas import department is 180 ℃ -240 ℃, then the reaction bed includes decarbonization bed and denitration bed, by the flue gas import to the exhanst gas outlet has set gradually a plurality of denitration bed and a plurality of decarbonization bed, the heat transfer import sets up in the upper reaches of first decarbonization bed, it is first to spout the setting of ammonia equipment the upper reaches of denitration bed, it is a plurality of grid reposition of redundant personnel pipe from top to bottom sets up respectively in a plurality of the upper reaches of decarbonization bed.
Further, in the above-mentioned synchronous decarbonization denitration of industrial flue gas and waste heat recovery utilize's device, if the temperature of flue gas inlet department is 240 ℃ -280 ℃, then the reaction bed includes the denitration decarbonization bed, from the flue gas inlet to the exhanst gas outlet sets gradually a plurality ofly the denitration decarbonization bed, the heat transfer import sets up first the upper reaches of denitration decarbonization bed, ammonia injection equipment sets up first the upper reaches of denitration decarbonization bed, and is a plurality of reposition of redundant personnel grid pipe sets up respectively from top to bottom in a plurality of the upper reaches of denitration decarbonization bed.
Further, in foretell synchronous decarbonization of industry flue gas denitration and waste heat recovery utilize's device, still include the two-way valve, work as in the decarbonization denitration tower by the flue gas import extremely the exhanst gas outlet has set gradually a plurality ofly decarbonization bed and a plurality of during the denitration bed, the two-way valve is provided with threely, and is three the two-way valve is first valve, second valve and third valve respectively, first valve sets up in the decarbonization bed with between the decarbonization bed on the circulation pipeline, the second valve sets up on the heating pipe, the third valve sets up on the back flow, when by the flue gas that the flue gas import got into need heat and keep warm, close first valve with the third valve opens second valve, circulation liquid absorbs can be right behind the heat of decarbonization bed the heating pipe is right flue gas in the flue gas pipeline heats, when the temperature of denitration bed is less than denitration catalytic activation temperature, close the second valve with the third valve opens first valve, circulation liquid absorption bed can be right after the heat of decarbonization bed the denitration bed heats the liquid storage tank is all closed by the heat of denitration catalyst with the second valve, the heat of second valve with the heat of second valve is heated and is passed through the heat of the circulation tank after the decarbonization bed.
The device can synchronously decarbonize and denitrate the industrial flue gas and recycle the waste heat generated in the decarbonizing process. Compared with the prior art, the technical scheme of the invention simultaneously carries out decarburization and denitration 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. The invention can effectively recover the redundant heat generated by decarburization, can powerfully ensure the normal operation of denitration, and simultaneously, the recovered heat can also be used for heating or insulating the flue gas entering from the flue gas inlet, thereby reducing the investment of flue gas heating equipment, keeping the temperature of the inlet flue gas stable and being beneficial to decarburization. The invention can not only synchronously decarbonize and denitrate, but also use the residual heat for other applications according to the actual conditions, thereby achieving double benefit effects.
Drawings
The exemplary embodiments and descriptions of the present invention are provided to explain the present invention and not to limit the present invention. Wherein:
FIG. 1 is a schematic structural diagram of an embodiment of the present invention (decarbonization followed by denitration).
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 the coil pipes in the reaction bed according to one embodiment of the present invention.
Fig. 4 is a schematic structural diagram of a shunt grid tube according to an embodiment of the present invention.
FIG. 5 is a schematic structural diagram of a decarbonizing and denitrating tower according to an embodiment of the present invention (denitrating and then decarbonating).
FIG. 6 is a schematic view of a decarbonizing and denitrating tower according to an embodiment of the present invention.
Description of reference numerals: 1, a decarburization and denitrification tower; 2, reacting a bed layer; 3, decarbonizing a bed layer; 4, denitrating a bed layer; 5, denitrating and decarbonizing a bed layer; 6, a flue gas inlet; 7, a smoke outlet; 8, a heat exchange inlet; 9 a first heat exchange outlet; 10 ammonia water inlet; 11 ammonia water line; 12 an atomizing nozzle; 13 a circulation line; 14 a liquid storage tank; 15 a coiled tube; 16 split flow grid tubes; 17 a first gas detection port; 18 first gas detection means; 19 temperature detection points; 20 a first temperature device; 21 a liquid level meter; 22 liquid injection port; 23 a pressure relief vent; 24 drain valves; 25 output pump; 26 discharging the pipe; 27 a second temperature device; 28 a second gas detection port; 29 a first valve; 30 a second valve; 31 a third valve; 32 heating pipes; 33 a return pipe; 34 a flue gas duct; 35 second heat exchange outlet.
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments. The various examples are provided by way of explanation of the invention, and not limitation of the invention. In fact, it will be apparent to those skilled in the art that modifications and variations can be made in the present invention without departing from the scope or spirit thereof. For instance, features illustrated or described as part of one embodiment, can be used with another embodiment to yield a still further embodiment.
In the description of the present invention, the terms "longitudinal", "lateral", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, which are for convenience of description of the present invention only and do not require that the present invention must be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. The terms "connected," "connected," and "disposed" as used herein are intended to be broadly construed, and may include, for example, fixed connections and removable connections; can be directly connected or indirectly connected through intermediate components; the connection may be a wired electrical connection, a wireless electrical connection, or a wireless communication signal connection, and a person skilled in the art can understand the specific meaning 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 similar designations in the drawings and description have been used to refer to like or similar parts of the invention. As used herein, the terms "first," "second," and "third," etc. may be used interchangeably to distinguish one component from another, and are not intended to denote position or importance of the individual components.
As shown in fig. 1 to fig. 6, according to an embodiment of the present invention, there is provided an apparatus for synchronous decarbonization and denitration and waste heat recovery of industrial flue gas, the apparatus including: the decarbonization and denitration tower comprises a decarbonization and denitration tower 1, ammonia spraying equipment and reaction beds 2, wherein the decarbonization and denitration tower 1 is a cylindrical tower body structure for example, the decarbonization and denitration tower 1 can also adopt other shapes such as a square tower body according to actual conditions, the decarbonization and denitration tower 1 is provided with a flue gas inlet 6 and a flue gas outlet 7, a flue gas pipeline 34 is connected with the flue gas inlet 6, industrial flue gas sequentially enters the decarbonization and denitration tower 1 through the flue gas pipeline 34 and the flue gas inlet 6, a plurality of reaction beds 2 are arranged in the decarbonization and denitration tower 1, the reaction beds 2 are located between the flue gas inlet 6 and the flue gas outlet 7, the industrial flue gas enters from the flue gas inlet 6 and is discharged from the flue gas outlet 7 after flowing through the reaction beds 2, and the industrial flue gas is synchronously decarbonized and denitrated in the process of flowing through the reaction beds 2. In the technical scheme of the invention, the number of the reaction bed layers 2 for decarburization, denitration or simultaneous decarburization and denitration is not limited, and the number of the reaction bed layers 2 can be determined according to the actual situation. Be provided with heat transfer import 8 and first heat transfer export 9 on the lateral wall of decarbonization denitration tower 1, be provided with aqueous ammonia entry 10 on the lateral wall of decarbonization denitration tower 1, spout ammonia equipment setting in decarbonization denitration tower 1, aqueous ammonia entry 10 with spout ammonia equipment intercommunication, spout ammonia equipment and can spout the aqueous ammonia, NO in the reduction flue gas under the effect of catalyst material after the aqueous ammonia atomizing X . In the decarbonization process, CO is oxidized to CO 2 Release unnecessary heat and heat the flue gas, if this part of heat does not utilize, can cause thermal waste, and influence the denitration, the flue gas that is heated flows into denitration bed 4, makes denitration bed 4 intensifies, can lead to the denitration effect to worsen when the temperature of denitration bed 4 has surpassed the normal use temperature of denitration catalyst. The technical scheme of the invention can realize the heating of the denitration bed layer 4Good regulation and control ensures that the denitration reaction of the denitration bed layer 4 is normally carried out, and can realize the resource utilization of the redundant heat of the decarburization bed layer 3.
Further, in the technical scheme of the invention, carbon refers to CO, nitre refers to NO X The concentration of CO in the flue gas entering the decarburization denitration tower 1 from the flue gas inlet 6 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 2 are all formed catalysts. The decarbonization and denitration tower 1 can generate waste heat in the decarbonization process, the utilization amount of the waste heat is determined according to the temperature rise condition of a decarbonization bed layer 3 brought by heat released by CO catalytic oxidation in the actual decarbonization reaction process, wherein the temperature rise quantity delta T of flue gas caused by the CO catalytic oxidation is as follows:
△T=
according to the CO catalytic oxidation process, the following steps are provided:
W＝Q•C•f•η
f＝a•GHSV+k
GHSV＝Q/V
to obtain: Δ T =
Wherein: q: flue gas flow rate; cp: specific heat capacity of flue gas; Δ T: the variation of the flue gas temperature before and after CO catalytic oxidation of the decarbonization bed layer; f: CO catalytic oxidation conversion rate; a is a relation constant of the space velocity and the CO catalytic oxidation conversion rate in the decarburization and denitration tower, and is a negative value; k is a reaction constant of the space velocity and the CO catalytic oxidation conversion rate in the decarburization denitration tower and is a positive value; GHSV: the space velocity of the decarburization and denitrification tower is GHSV ∈ [2000,20000](ii) a V: the loading amount of the decarburization catalyst in the decarburization denitration tower; w: heat production of a decarburization bed in the decarburization and denitration tower; c: the concentration of CO in the flue gas; η: conversion of CO to CO at Unit flow 2 The amount of heat released.
CO(g)+1/2O 2 (g)=CO 2 (g) △H=-283.0KJ/mol
With a CO concentration of 15000mg/Nm 3 Flow Qm 3 H, catalyst 1m 3 Airspeed of 5000h -1 The specific heat capacity of the flue gas is about 1.2KJ/m 3 In the case of complete catalytic oxidation of CO (conversion 100%), the oxidation to CO is carried out in accordance with 1mol of CO 2 Can emit 283.0KJ of heat, then 15000mg/Nm 3 I.e., 0.54mol/Nm 3 The heat release rate is 152.8KJ/Nm 3 ，Qm 3 Conversion of CO to CO at a flow/h 2 When the heat release rate is 152.8 × qkj/h, the heat release rate is determined by the above formula Δ T =
The change of the temperature of the flue gas before and after CO catalytic oxidation of the decarbonization bed layer 3 is calculated to be about 127.3 ℃, namely the temperature of the flue gas can be theoretically raised by about 127.3 ℃ due to CO catalytic oxidation, so that the method has a flue gas waste heat utilization value.
Further, the device also comprises a circulating pipeline 13 and a liquid storage tank 14, an interlayer is arranged on the wall of the decarburization denitration tower 1, the circulating pipeline 13 is arranged in the interlayer, the circulating pipeline 13 needs to have certain characteristics of high temperature resistance, corrosion resistance, pressure resistance and the like, the diameter of the circulating pipeline 13 can be determined according to practical application conditions, heat insulation cotton or other heat insulation materials are filled in the interlayer for performing heat insulation on the inside of the decarburization denitration tower 1, two ends of the circulating pipeline 13 are respectively communicated with the liquid storage tank 14 through a heat exchange inlet 8 and a first heat exchange outlet 9, a coil pipe 15 is arranged at the bottom of part of the reaction bed 2, the coil pipe 15 is made of corrosion-resistant and high-temperature-resistant stainless steel, the coil pipe 15 is in direct contact with catalyst materials filled in the reaction bed 2, all the coil pipes 15 in the decarburization denitration tower 1 are sequentially communicated through the circulating pipeline 13, the circulating liquid in the circulating pipeline 13 can recover in situ excess heat generated by the catalyst materials in the decarburization process when flowing through the coil pipes 15 of the decarburization bed 3 or the denitration bed 5, and can ensure the in-situ heating effect of the catalyst when the circulating liquid in the bed 13 flows through the denitration bed 4. As shown in fig. 2 and 3, a coil pipe 15 is in the same plane and is spiral as a whole, the spiral coil pipe 15 has enough space to ensure the normal circulation of the flue gas, and the shape, size and pipe diameter of the coil pipe 15The non-fixed state can be determined according to the size of the space of the reaction bed layer 2 in the actual decarburization denitration tower 1 and the heat exchange effect. Be equipped with a plurality of reposition of redundant personnel grid pipes 16 in decarbonization denitration tower 1, the import and the export of reposition of redundant personnel grid pipe 16 all communicate with circulation pipeline 13, the material of reposition of redundant personnel grid pipe 16 is corrosion-resistant high temperature resistant stainless steel, be provided with the buckle on the tower wall of decarbonization denitration tower 1, reposition of redundant personnel grid pipe 16 arranges the upper reaches at decarbonization bed 3 through the buckle, reposition of redundant personnel grid pipe 16 and flue gas direct contact, for making the flue gas normal flow, reposition of redundant personnel grid pipe 16 leaves sufficient space, circulation liquid in circulation pipeline 13 not only accomplishes the normal position and retrieves decarbonization bed 3 and the unnecessary heat that produces at a large amount of oxidations of decarbonization in-process CO when shunting grid pipe 16 flows through, and can well shunt import flue gas, avoid simultaneously increase flue gas flow resistance, make the smooth circulation of flue gas, and then make catalyst material and flue gas fully contact reaction. The shape of the splitter grating tube 16 is not limited in the present invention, and in one embodiment of the present invention, as shown in fig. 4, the splitter grating tube 16 is composed of a plurality of horizontal tubes and a plurality of vertical tubes, the plurality of horizontal tubes are sequentially arranged, the plurality of vertical tubes are sequentially arranged above the plurality of horizontal tubes, and the plurality of horizontal tubes are sequentially connected and then communicated with the sequentially connected vertical tubes. In other embodiments of the present invention, the splitter grid tubes 16 may also be shaped in other ways. A first gas detection port 17 is arranged on the side wall of the decarburization denitration tower 1, a first gas detection device 18 is connected with the first gas detection port 17, and the first gas detection port 17 is used for detecting CO and CO in the flue gas in the decarburization denitration tower 1 2 、NO X （NO、NO 2 ) Is used to determine the oxidation of CO and NO during practical application X If the CO in the decarbonation and denitration tower 1 or at the flue gas outlet 7 is removed, for example, compared with the concentration value of the inlet flue gas 2 Higher concentration and NO X A lower concentration means a higher degree of CO oxidation, a better decarburization effect, and NO X The removal rate is high, and the denitration effect is good. A plurality of temperature detection points 19 are arranged in the decarburization denitration tower 1, the temperature detection points 19 are connected with a first temperature device 20 arranged outside the decarburization denitration tower 1, decarburization and denitration reaction are simultaneously carried out in the decarburization denitration tower 1, and first gas is detectedThe measuring device 18 and the first temperature device 20 can measure the temperature in the decarbonization and denitration tower 1 and the CO and NO in the flue gas X The content of (b) is detected from time to time. The flow direction of the circulating liquid is determined according to the detection result of the first temperature device 20 on the temperature of each temperature detection point 19 in the decarburization denitration tower 1, and the purpose of heating and heat preservation of the flue gas in the flue gas pipeline 34 or heating the catalyst material in the denitration bed 4 can be realized by changing the flow direction of the circulating liquid.
Further, the liquid storage tank 14 is a tank body for storing a certain volume of circulating liquid, wherein the circulating liquid can be water or appropriate material components such as heat conduction oil, and the circulating liquid can absorb and recycle heat generated by the catalyst material in the decarburization denitration tower 1 during the decarburization process by circulating between the decarburization denitration tower 1 and the liquid storage tank 14. Be provided with level gauge 21 on the lateral wall of liquid reserve tank 14, level gauge 21 is used for monitoring the liquid level of the circulation liquid in the liquid reserve tank 14, the top of liquid reserve tank 14 is provided with notes liquid mouth 22 and pressure release mouth 23, it is used for supplementing circulation liquid to liquid reserve tank 14 to annotate liquid mouth 22, pressure release mouth 23 is used for releasing unnecessary pressure in the liquid reserve tank 14, in order to guarantee device's normal operating, the bottom of liquid reserve tank 14 is provided with flowing back valve 24, be provided with output pump 25 on the pipeline between liquid reserve tank 14 and heat transfer import 8, circulation pipeline 13 is linked together with output pump 25 through heat transfer import 8, output pump 25 is arranged in sending circulation liquid into 1 inner circulation pipeline 13 of decarbonization denitration tower smoothly, and realize the circulation. Circulation pipeline 13 in decarbonization denitration tower 1 is connected with reposition of redundant personnel grid pipe 16, coiled pipe 15 respectively, whether need give heating and heat preservation and whether need give the catalyst material heating and heat preservation of denitration bed 4 to the flue gas that flue gas inlet 6 got into according to needs, and final circulation liquid has three flow direction respectively, and first flow direction is to flue gas pipeline 34 with flue gas inlet 6 is connected, and second flow is to denitration bed 4, and third is the direct flow back to liquid reserve tank 14, and specific selection which flow direction can be decided according to actual reaction temperature demand condition. After absorbing heat, the circulating liquid utilizes the liquid storage tank 14 to store the heat, and the liquid storage tank 14 can also be connected with other equipment needing heat supply and supply heat to other equipment needing heat supply so as to recycle waste heat.
Further, the air conditioner is provided with a fan,spout ammonia equipment and include ammonia water pipeline 11 and atomizer 12, ammonia water pipeline 11 is used for the ammonia water entry 10 and the 12 intercommunication of atomizer, and atomizer 12 can spout the ammonia water and make the ammonia water atomizing, and the ammonia water atomizing back fully contacts with the catalyst material that is used for the denitration, reduces the NO in the flue gas under the effect of catalyst material X And the first heat exchange outlet 9 is arranged at the downstream of all the reaction beds 2, and the flow direction of the circulating liquid in the decarburization denitration tower 1 is from top to bottom, so that the flowing resistance of the circulating liquid can be reduced.
Further, the flue gas inlet 6 is located the top of the decarburization denitration tower 1, the flue gas outlet 7 is located the bottom of the decarburization denitration tower 1, the flue gas outlet 7 is communicated with a discharge pipe 26, the flue gas enters the decarburization denitration tower 1 from the flue gas inlet 6 and 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 are connected with the second gas detection port 28, and 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 CO and NO and the temperature of the flue gas discharged from the flue gas outlet 7 X The content of (b) is detected.
Further, if the temperature of flue gas at the flue gas inlet 6 is 100 ℃ -180 ℃, as shown in fig. 1, the reaction bed 2 comprises a decarburization bed 3 and a denitration bed 4, the order of decarburization and denitration of the flue gas in the decarburization and denitration tower 1 is decarburization and denitration, a plurality of decarburization beds 3 and a plurality of denitration beds 4 are sequentially arranged from the flue gas inlet 6 to the flue gas outlet 7, the heat exchange inlet 8 is arranged at the upstream of the first decarburization bed 3, and the atomizing nozzle 12 of the ammonia injection device is arranged at the upstream of the first denitration bed 4, namely: the atomizing nozzle 12 of the ammonia spraying equipment is arranged at the middle position of the gap between the decarburization bed layer 3 and the denitration bed layer 4, so that the ammonia water sprayed out by the atomizing nozzle 12 can be prevented from being excessively oxidized by the high-temperature flue gas of the decarburization bed layer 3, the ammonia water can be fully contacted with the catalyst material in the denitration bed layer 4 after atomization, and the denitration effect is ensured. The plurality of flow distribution grid pipes 16 are respectively arranged at the upstream of the plurality of decarburization beds 3 from top to bottom, in an embodiment of the invention, two flow distribution grid pipes 16 are arranged, the two flow distribution grid pipes 16 are respectively arranged at the upstream of the first decarburization bed 3 and the second decarburization bed 3, a second heat exchange outlet 35 is arranged on the side wall of the decarburization denitration tower 1 between the plurality of decarburization beds 3 and the plurality of denitration beds 4, the circulating pipeline 13 is communicated with both the second heat exchange outlet 35, the second heat exchange outlet 35 is communicated with a heating pipe 32 and a return pipe 33, the return pipe 33 is communicated with the liquid storage tank 14, the heating pipe 32 passes through a flue gas pipeline 34, and the heating pipe 32 is used for heating flue gas entering the flue gas inlet 6 from the flue gas pipeline 34.
Further, if the temperature of flue gas at the flue gas inlet 6 is 180 ℃ -240 ℃, the reaction bed 2 comprises a decarburization bed 3 and a denitrification bed 4, the order of decarburization and denitrification of the flue gas in the decarburization and denitrification tower 1 is denitrification before decarburization, a plurality of denitrification beds 4 and a plurality of decarburization beds 3 are sequentially arranged from the flue gas inlet 6 to the flue gas outlet 7, the heat exchange inlet 8 is arranged at the upstream of the first decarburization bed 3, the atomizing nozzle 12 of the ammonia injection device is arranged at the upstream of the first denitrification bed 4, and the plurality of shunt grid pipes 16 are respectively arranged at the 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 6 flue gases of flue gas inlet is 240 ℃ -280 ℃, then reaction bed 2 includes denitration decarbonization bed 5, the flue gas is the decarbonization denitration simultaneously in decarbonization denitration tower 1, a plurality of denitration decarbonization bed 5 have been set gradually by flue gas inlet 6 to exhanst gas outlet 7, heat transfer import 8 sets up the upper reaches at first denitration decarbonization bed 5, the atomizing nozzle 12 of ammonia injection equipment sets up the upper reaches at first denitration decarbonization bed 5, a plurality of reposition of redundant personnel grid pipes 16 set up the upper reaches at a plurality of denitration decarbonization bed 5 from top to bottom respectively. In one embodiment, as shown in fig. 6, six denitrification and decarburization beds 5 are arranged.
Furthermore, the device also comprises a two-way valve which is a control valve with high temperature resistance, corrosion resistance and flexible operation, and the two-way valve is used for controlling the flow direction of the circulating liquid in the circulating pipeline 13 and finally controlling the flow direction of the circulating liquid which flows through the decarburization bed 3 and has the recovered heat by opening or closing the two-way valve. According to whether need give the flue gas that 6 flue gas intakes got into heat and keep warm and whether need give the catalyst material heating and the heat preservation of denitration bed 4, the circulating liquid finally has three flow direction respectively, and first the flow direction is to flue gas pipeline 34 with import flue gas coupling, second flow direction denitration bed 4, and third is the direct flow back to liquid reserve tank 14, and it can be decided according to actual reaction temperature demand condition to specifically select which flow direction.
For the inlet flue gas temperature of 180 ℃ -240 ℃ denitration and decarburization, and the simultaneous decarburization and denitration at 240 ℃ -280 ℃ are carried out by adjusting the upper and lower positions of the ammonia injection equipment, the circulation pipeline 13, the coil pipe 15 and the flow dividing grid pipe 16 on the basis of the device used for the inlet flue gas temperature of 100 ℃ -180 ℃ denitration and decarburization.
Example 1:
in this embodiment, the temperature of the flue gas at the flue gas inlet 6 is 100 ℃ -180 ℃, the order of decarbonization and denitration of the flue gas in the decarbonization and denitration tower 1 is decarbonization first and denitration second, as shown in fig. 1, two decarbonization bed layers 3 and four denitration bed layers 4 are sequentially arranged from the flue gas inlet 6 to the flue gas outlet 7, the decarbonization bed layers 3 are filled with a catalyst specially used for decarbonization, and the denitration bed layers 4 are filled with a catalyst specially used for denitration. The two shunt grid pipes 16 are arranged, the two shunt grid pipes 16 are respectively arranged at the upstream of the two decarburization beds 3, and the atomizing nozzle 12 of the ammonia spraying device is arranged at the upstream of the first denitration bed 4. Two temperature detection points 19 are arranged, one temperature detection point 19 is arranged between the two decarburization beds 3, the other temperature detection point 19 is arranged between the second denitration bed 4 and the third denitration bed 4, and each temperature detection point 19 is connected with a first temperature device 20. The first gas detection port 17 is provided between the first denitration bed 4 and the second denitration bed 4. Two denitration beds 3, the bottom of third denitration bed 4 and fourth denitration bed 4 all is provided with coiled pipe 15, coiled pipe 15 and reposition of redundant personnel grid pipe 16 in the decarbonization bed 3 are used for absorbing the waste heat that produces at the in-process of decarbonization, coiled pipe 15 in the denitration bed 4 is used for being used for heating the catalyst material in the denitration bed 4, because first denitration bed 4 and second denitration bed 4 all are close to decarbonization bed 3, although can utilize circulation liquid in the coiled pipe 15 of decarbonization bed 3 to retrieve most heat, but also can heat the part flue gas, make the flue gas heat up, when the flue gas gets into first denitration bed 4 and second denitration bed 4, the flue gas temperature is enough high, the flue gas temperature can ensure going on of denitration reaction, the catalyst material does not need the heat supply, when the flue gas passes through third denitration bed 4 and fourth denitration bed 4, the flue gas temperature descends, lower flue gas temperature does not utilize the denitration, consequently, need not set up coiled pipe 15 in first denitration bed 4 and second denitration bed 4, and denitration bed 4 and fourth denitration bed 4 in need set up coiled pipe 15.
In the present embodiment, three two-way valves are provided, the three two-way valves are a first valve 29, a second valve 30 and a third valve 31, the first valve 29 is provided on the circulation line 13 between the first denitration bed 4 and the second denitration bed 4, the second valve 30 is provided on the heating pipe 32, and the third valve 31 is provided on the return pipe 33. The first temperature device 20 is connected with 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, and the first temperature device 20 can automatically control the first valve 29, the second valve 30 and the third valve 31 according to the monitoring value of the temperature detection point 19, so as to control the flow direction of the circulating liquid in the circulating pipeline 13. The first valve 29, the second valve 30 and the third valve 31 can be controlled manually according to the gas concentration 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 liquid. The number and the position of the two-way valves are not fixed and can be flexibly changed, but the three flow directions of the final circulating liquid need to be kept unchanged.
When the flue gas entering from the flue gas inlet 6 needs to be heated and heat-preserved, the first valve 29 and the third valve 31 are closed, the second valve 30 is opened, the circulating liquid flows out from the liquid storage tank 14 through the output pump 25, sequentially passes through the heat exchange inlet 8, the circulating pipeline 13, the shunt grid pipe 16, the coil pipe 15 and the second heat exchange outlet 35 in the decarburization bed 3, and then flows to the flue gas pipeline 34 through the heating pipe 32, and the circulating liquid can heat the flue gas entering from the flue gas inlet 6 through the heating pipe 32 after absorbing the heat of the decarburization bed 3. 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, the circulating liquid flows out from the liquid storage tank 14 through the output pump 25, sequentially flows through the heat exchange inlet 8, the circulating pipeline 13, the shunt grid pipe 16, the disc pipe 15 in the denitration bed layer 3, the disc pipe 15 in the third denitration bed layer 4, the disc pipe 15 in the fourth denitration bed layer 4 and the second heat exchange outlet 35, flows back to the liquid storage tank 14 to complete circulation, and after absorbing the heat of the denitration bed layer 3, the circulating liquid can heat the corresponding denitration bed layer 4 when flowing through the disc pipe 15 in the denitration bed layer 4. When the flue gas entering from the flue gas inlet 6 and the catalyst of the denitration bed 4 do not need heating and heat preservation, the first valve 29 and the second valve 30 are closed, the third valve 31 is opened, the circulating liquid flows out from the liquid storage tank 14 through the output pump 25, sequentially passes through the heat exchange inlet 8, the circulating pipeline 13, the shunt grid pipe 16, the coiled pipe 15 and the first heat exchange outlet 9 in the decarburization bed 3, then flows back to the liquid storage tank 14 through the return pipe 33 to complete circulation, and the circulating liquid absorbs the heat of the decarburization bed 3 and then flows back to the liquid storage tank 14 through the return pipe 33 to be stored.
In this embodiment, when the first temperature device 20 detects that the temperature of the decarbonization bed layer 3 is high and exceeds 180 ℃, the first temperature device 20 automatically controls the first valve 29, the second valve 30 and the third valve 31 to make the circulating liquid flow into the denitration bed layer 4 below the decarbonization and denitration tower 1, so that the temperature of the denitration bed layer 4 reaches the temperature required for denitration, thereby satisfying normal denitration. If the first gas detection port 17 and the second gas detection port 28 detect NO at the outlet of the decarburization denitration tower 1 X Concentration is higher, then means that denitration efficiency is lower, can make the circulating liquid flow in denitration bed 4 through the flow direction of artificial mode control circulating liquid, improves denitration bed 4's temperature, finally improves denitration efficiency.
In this embodiment, can realize denitration also can realize the decarbonization in a decarbonization denitration tower 1, the produced heat of while decarbonization in-process can also carry out abundant utilization through the mode of circulating liquid, that is to say realizes waste heat utilization, the heat that will utilize can be used for heating up the inlet flue gas also can give denitration bed 4 heat supply, when neither needs this part of heat, can carry out reserve or give other heating equipment with the heat of retrieving and supply heat.
Example 2:
in this embodiment, as shown in fig. 5, the temperature of the flue gas at the flue gas inlet 6 is 180 ℃ to 240 ℃, the order of the decarbonization and denitrification of the flue gas in the decarbonization and denitrification tower 1 is denitrification before decarburization, two denitrification beds 4 and four decarbonization beds 3 are sequentially arranged from the flue gas inlet 6 to the flue gas outlet 7, the decarbonization beds 3 are filled with a catalyst specially used for decarbonization, and the denitrification beds 4 are filled with a catalyst specially used for denitrification. Two shunt grating pipes 16 are arranged, and the two shunt grating pipes 16 are respectively arranged at the upstream of the first decarburization bed layer 3 and the upstream of the second decarburization bed layer 3. The atomizing nozzle 12 of the ammonia injection device is arranged at the upstream of the first denitration bed layer 4. One temperature detection point 19 is arranged, the temperature detection point 19 is arranged between the second denitration bed layer 4 and the first decarburization bed layer 3, and the temperature detection point 19 is connected with a first temperature device 20. The bottom parts of the first decarburization bed 3, the second decarburization bed 3 and the third decarburization bed 3 are all provided with a coil pipe 15, and the coil pipe 15 and the shunt grid pipe 16 in the decarburization bed 3 are used for absorbing the waste heat generated in the decarburization process. Because denitration bed 4 is close to flue gas inlet 6, the temperature of flue gas can guarantee that denitration bed 4 normally realizes the denitration, needn't supply heat for the catalyst material of denitration bed 4, consequently does not set up coil pipe 15 in denitration bed 4. The heat that three decarbonization bed 3 oxidation above the fourth decarbonization bed 3 released, after the most heat is retrieved to the circulating fluid, remaining heat can carry out the intensification of certain degree for the flue gas, when the flue gas reachd the fourth decarbonization bed 3, the temperature is enough to carry out normal decarbonization, and fourth decarbonization bed 3 is in the bottom of decarbonization denitration tower 1, consider probably not to release a large amount of heat again, so neither carry out waste heat utilization nor supply the heat to fourth decarbonization bed 3, consequently fourth decarbonization bed 3 does not set up coil pipe 15.
In this embodiment, the circulating liquid has only one flow direction, the circulating liquid flows out from the liquid storage tank 14 through the output pump 25, and directly flows back to the liquid storage tank 14 after sequentially passing through the heat exchange inlet 8, the circulating pipeline 13, the shunt grid pipe 16, the coiled pipe 15 in the decarbonizing bed layer 3 and the first heat exchange outlet 9, and the heat of the decarbonizing bed layer 3 absorbed by the circulating liquid is stored in the liquid storage tank 14. The first temperature device 20 monitors the temperature of the denitration bed 4 and the first gas detection port 17 and the second gas detection portNO detection by two gas detection port 28 X Is in accordance with the concentration value of NO X When the removal efficiency is high, the heat of the decarburization bed 3 is collected by the circulating liquid and then flows back to the liquid storage tank 14 for standby or supplies heat to other equipment needing heat supply, and the heat supply to the inlet flue gas and the denitration bed 4 is not needed.
Example 3:
in this embodiment, as shown in fig. 6, the temperature of the flue gas at the flue gas inlet 6 is 240 to 280 ℃, the order of decarburization and denitration of the flue gas in the decarburization and denitration tower 1 is simultaneous decarburization and denitration, six denitration and decarburization beds 5 are sequentially arranged from the flue gas inlet 6 to the flue gas outlet 7, the decarburization catalyst and the denitration catalyst in the denitration and decarburization beds 5 may be the same catalyst or different catalysts, which can be determined according to actual application conditions, and the final purpose is to synchronously realize decarburization and denitration. The number of the two shunt grid pipes 16 is two, and the two shunt grid pipes 16 are respectively arranged at the upstream of the first denitration and decarburization bed layer 5 and the upstream of the second denitration and decarburization bed layer 5. The ammonia spraying equipment is arranged at the upstream of the first denitration and decarbonization bed layer 5. One temperature detection point 19 is arranged, the temperature detection point 19 is arranged at the upstream of the first denitration and decarburization bed 5, and the temperature detection point 19 is connected with a first temperature device 20. The bottom of the first denitration and decarburization bed 5, the second denitration and decarburization bed 5 and the third denitration and decarburization bed 5 are respectively provided with a coil pipe 15, and the coil pipes 15 and the shunt grid pipes 16 in the denitration and decarburization bed 5 are used for absorbing the waste heat generated in the decarburization process.
In this embodiment, the circulating liquid has only one flow direction, the circulating liquid flows out from the liquid storage tank 14 through the output pump 25, and directly flows back to the liquid storage tank 14 after sequentially passing through the heat exchange inlet 8, the circulating pipeline 13, the flow dividing grid pipe 16, the disk-shaped pipe 15 in the denitration and decarbonization bed layer 5 and the first heat exchange outlet 9, and the heat of the denitration and decarbonization bed layer 5 absorbed by the circulating liquid is stored in the liquid storage tank 14. As CO is greatly oxidized during the decarburization of the denitration and decarburization bed layer 5, the temperature of the denitration and decarburization bed layer 5 rises, so that the temperature measured by the first temperature device 20 is higher than the temperature required by the denitration and decarburization bed layer 5 for denitration, and NO at the tower outlet detected by the first gas detection port 17 and the second gas detection port 28 X Higher concentration value and lower denitration efficiencyThe temperature of the denitration and decarbonization bed layer 5 is reduced by utilizing the circulating liquid so as to meet the temperature requirement of simultaneous decarburization and denitration.
From the above description, it can be seen that the above-described embodiments of the present invention achieve the following technical effects:
the utility model provides a synchronous decarbonization denitration of industrial flue gas and waste heat recovery utilize's device, utilizes the device can carry out recycle to the waste heat that the decarbonization in-process produced to the synchronous decarbonization denitration of industrial flue gas to.
Compared with the prior art, the technical scheme of the invention can dynamically adjust the arrangement in the decarburization and denitration tower 1 according to the temperature of the flue gas, and perform decarburization and denitration in the decarburization and denitration tower 1 simultaneously, thereby greatly saving the equipment investment of step-by-step treatment, reducing the occupied area and saving the cost and the operating cost. The invention realizes the resource utilization of waste heat by effectively recovering the redundant heat generated by decarburization, powerfully ensures the normal operation of denitration, and simultaneously the recovered heat can also be used for heating or insulating the flue gas entering from the flue gas inlet 6, thereby reducing the investment of flue gas heating equipment, keeping the temperature of the inlet flue gas stable and being beneficial to decarburization. The technical scheme of the invention not only can synchronously decarbonize and denitrate, but also can use the residual heat for other uses according to the actual situation, thereby playing a dual-benefit effect.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in 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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| CN103307622A (en) * | 2013-07-05 | 2013-09-18 | 宜兴天地节能技术有限公司 | Desulfurization, denitrification and decarburization integrated system for high-efficiency energy-saving environment-friendly industrial boiler |
| CN205360958U (en) * | 2016-02-03 | 2016-07-06 | 青岛农业大学 | Modular integrated device of flue gas desulfurization denitration decarbonization |
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| AT10369U1 (en) * | 2008-01-16 | 2009-02-15 | Kirchdorfer Zementwerk Hofmann | FUMES CLEANING SYSTEM |
| CN105314595B (en) * | 2014-07-11 | 2018-03-20 | 中国石油化工股份有限公司 | CO transformationreation stoves |
| CN105233672A (en) * | 2015-11-05 | 2016-01-13 | 云南蓝澈科技有限公司 | Denitration and decarburization device for sintering flue gas and process thereof |
| CN206240324U (en) * | 2016-10-31 | 2017-06-13 | 昆明理工大学 | It is a kind of to remove cos, carbon disulfide device simultaneously |
| CN112403218B (en) * | 2019-11-05 | 2022-05-03 | 中冶长天国际工程有限责任公司 | Flue gas decarburization and denitration treatment system and method |
| CN112403224B (en) * | 2019-11-06 | 2022-01-25 | 中冶长天国际工程有限责任公司 | CO oxidation and denitration system and method |
| CN111664717B (en) * | 2020-05-25 | 2022-07-01 | 中钢集团天澄环保科技股份有限公司 | Intelligent catalytic denitration CO removal and waste heat utilization integrated device |
| CN112902680A (en) * | 2021-01-29 | 2021-06-04 | 中冶华天南京工程技术有限公司 | Sintering flue gas SCR denitration energy-saving emission-reducing method and system |
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| CN103307622A (en) * | 2013-07-05 | 2013-09-18 | 宜兴天地节能技术有限公司 | Desulfurization, denitrification and decarburization integrated system for high-efficiency energy-saving environment-friendly industrial boiler |
| CN205360958U (en) * | 2016-02-03 | 2016-07-06 | 青岛农业大学 | Modular integrated device of flue gas desulfurization denitration decarbonization |
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