CN115554826A - Flue gas desulfurization, denitration, dust removal and decarbonization system - Google Patents
Flue gas desulfurization, denitration, dust removal and decarbonization system Download PDFInfo
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Abstract
The utility model provides a flue gas desulfurization, denitration, dust removal and decarbonization system, belongs to industry flue gas treatment facility technical field, and along flue gas treatment process order, flue gas desulfurization, denitration, dust removal and decarbonization system are including connecting gradually: the system comprises a desulfurization subsystem, a dust removal subsystem, a decarburization subsystem and a denitration subsystem; and two treated flue gas branches which are arranged in parallel, wherein one branch is connected with the chimney, and the other branch is connected with the carbon dioxide desorption subsystem. The invention realizes the desulfurization, denitration, dust removal and decarburization of the flue gas by organically structuring each subsystem. According to the invention, a small amount of denitrated clean flue gas can be extracted to desorb the supplement-collecting agent which collects carbon dioxide, so that carbon dioxide gas with high purity and high concentration is obtained for reuse. The original desulfurization, denitration and dust removal system of the flue gas is integrated with a newly-built carbon dioxide adsorption and desorption system, so that the one-time investment is saved, and the energy cost required in the desorption process is saved.
Description
Technical Field
The invention relates to the technical field of industrial flue gas treatment equipment, in particular to a flue gas desulfurization, denitration, dust removal and decarburization system.
Background
Industrial flue gas as CO 2 Relates to a plurality of fields such as metallurgy, electric power, chemical industry, machinery, internal combustion engines and the like. In all flue gas discharged by a steel plant, the amount of sintering (pelletizing) flue gas accounts for about 80%, and the realization of the double-carbon target in the steel industry mainly depends on the emission reduction of carbon dioxide in the sintering (pelletizing) flue gas.
CO 2 Post-combustion capture refers to capture of CO in flue gas using a suitable method 2 And the post-combustion capture system can be added directly to existing industrial plant systems without the need for extensive retrofit processes. At present, the post-combustion trapping technology is mainly an absorption method, the absorption method becomes one of the main means for reducing emission of the current industrial equipment by means of a relatively mature technology, but the energy consumption of the regeneration process of the absorbent is high. Secondly, most industrial flue gas carbon dioxide capture systems are used as newly-built flue gas treatment systems (carbon dioxide complementary collection systems), which cannot be uniformly combined with the traditional flue gas desulfurization system, the traditional denitration system and the traditional dedusting system and only can be operated independently.
Although the prior art provides an industrial flue gas carbon dioxide capture system (Chinese patent with application number CN 110683545A), the system realizes CO in flue gas by adopting heat exchange, water removal, compression, precooling, recooling and deep cooling processes 2 The process of the trapping is too complex, so that the construction cost and the operation cost of the whole system are very high.
Disclosure of Invention
Problem (A)
In summary, how to provide a flue gas treatment system with low operation cost and high removal rate of carbon dioxide becomes a problem to be solved by those skilled in the art.
(II) technical scheme
In order to achieve the above purpose, the invention provides the following technical scheme:
the invention provides a flue gas desulfurization, denitration, dust removal and decarburization system. In the invention, along the sequence of the flue gas treatment process, the flue gas desulfurization, denitration, dust removal and decarburization system comprises the following components in sequential connection:
a desulfurization subsystem for implementing flue gas desulfurization;
a dust removal subsystem for realizing the dust removal of the flue gas;
the decarbonization subsystem is used for removing carbon dioxide from the flue gas;
a denitration subsystem for realizing the denitrification of the flue gas;
and two treated flue gas branches arranged in parallel, wherein one treated flue gas branch is connected with a chimney for discharging treated flue gas, the other treated flue gas branch is connected with a carbon dioxide desorption subsystem, the carbon dioxide desorption subsystem is in process connection with the decarburization subsystem and is used for receiving the carbon dioxide capturing agent adsorbed with carbon dioxide and carrying out carbon dioxide desorption operation on the carbon dioxide capturing agent;
wherein the temperature range of the flue gas output by the dedusting subsystem is 40-55 ℃, and the temperature range of the flue gas output by the denitration subsystem is 110-130 ℃.
Preferably, in the flue gas desulfurization, denitration, dust removal and decarburization system provided by the invention, the desulfurization subsystem is a wet desulfurization system; the desulfurization subsystem comprises a pre-desulfurizer preparation subsystem for preparing a desulfurizer, a desulfurization tower connected with the pre-desulfurizer preparation subsystem for receiving the desulfurizer and a desulfurization post-treatment subsystem; the flue gas is washed by a desulfurizer in the desulfurizing tower to be saturated flue gas, and the temperature is reduced from 120-180 ℃ to 50-60 ℃.
Preferably, in the flue gas desulfurization, denitration, dust removal and decarburization system provided by the invention, the dust removal subsystem is a wet electric dust remover.
Preferably, in the flue gas desulfurization, denitration, dust removal and decarburization system provided by the invention, a condensing subsystem is further arranged between the desulfurization subsystem and the dust removal subsystem; the condensation subsystem comprises a cooling tower, a condenser is arranged in the cooling tower, a circulating water pool is connected with the condenser, and a circulating water pump is arranged on a cooling water circulating pipeline formed by the condenser and the circulating water pool; the flue gas is changed into saturated flue gas by heat exchange with cooling water in a condenser, and the temperature is reduced from 50-60 ℃ to 40-55 ℃.
Preferably, in the system for desulfurizing, denitrating, dedusting and decarbonizing flue gas provided by the invention, the decarbonizing subsystem comprises an adsorption tower, a capturing agent bed layer for dispersing a carbon dioxide capturing agent is arranged in the adsorption tower, a capturing agent inlet for inputting the carbon dioxide capturing agent, a capturing agent outlet for outputting the carbon dioxide capturing agent, flue gas inlet for inputting flue gas and a flue gas outlet for outputting flue gas are arranged on the adsorption tower.
Preferably, in the flue gas desulfurization, denitration, dust removal and decarburization system provided by the invention, the carbon dioxide desorption subsystem comprises an analysis tower, the analysis tower is provided with an analysis inlet and an analysis outlet, the direction in which the analysis inlet points to the analysis outlet is an analysis direction, an analysis path is formed in the analysis tower and along the analysis direction, and the analysis path comprises an analysis section.
Preferably, in the flue gas desulfurization, denitration, dust removal and decarburization system provided by the invention, the operating temperature range in the adsorption tower is 40-80 ℃; the operating temperature range of the resolving section is 110-130 ℃.
Preferably, in the system for desulfurizing, denitrating, dedusting and decarbonizing flue gas provided by the invention, the top of the adsorption tower is provided with the trapping agent inlet, the bottom of the adsorption tower is provided with the trapping agent outlet, the side wall of the adsorption tower and the position close to the top of the adsorption tower are provided with the flue gas outlet, and the side wall of the adsorption tower and the position close to the bottom of the adsorption tower are provided with the flue gas inlet; and the carbon dioxide trapping agent and the flue gas form countercurrent in the adsorption tower.
Preferably, in the system for desulfurization, denitration, dust removal and decarburization of flue gas provided by the invention, the desorption inlet is arranged at the top of the desorption tower, the desorption outlet is arranged at the bottom of the desorption tower, the desorption inlet is connected with the collector outlet through a conveying system, and the desorption outlet is butted with the collector inlet for recycling the carbon dioxide collector; and a desorption gas source inlet is formed in the side wall of the desorption tower and corresponds to the lower end of the desorption section, and a desorption gas rich gas outlet is formed in the side wall of the desorption tower and corresponds to the upper end of the desorption section.
Preferably, in the flue gas desulfurization, denitrification, dust removal and decarburization system provided by the invention, the denitrification subsystem is an SCR denitrification system.
(III) advantageous effects
The invention provides a flue gas desulfurization, denitration, dust removal and decarburization system, which comprises the following components in sequence along the process sequence of flue gas treatment: a desulfurization subsystem for implementing flue gas desulfurization; a dust removal subsystem for realizing the dust removal of the flue gas; the decarbonization subsystem is used for removing carbon dioxide from the flue gas; a denitration subsystem for realizing denitrification of the flue gas; and two treated flue gas branches arranged in parallel, wherein one treated flue gas branch is connected with a chimney for discharging treated flue gas, the other treated flue gas branch is connected with a carbon dioxide desorption subsystem, the carbon dioxide desorption subsystem is in process connection with the decarburization subsystem and is used for receiving the carbon dioxide capturing agent adsorbed with carbon dioxide and carrying out carbon dioxide desorption operation on the carbon dioxide capturing agent; wherein, the temperature range of the flue gas output by the dedusting subsystem is 40-55 ℃, and the temperature range of the flue gas output by the denitration subsystem is 110-130 ℃.
The system comprises a wet desulphurization system (desulphurization subsystem), a dust removal system (comprising a dust removal subsystem and a condensation subsystem), an SCR denitration system (denitration subsystem) and a dry adsorption and carbon dioxide removal system (decarburization subsystem and a carbon dioxide desorption subsystem), wherein flue gas is treated by the wet desulphurization system, the dust removal system, the carbon dioxide adsorption system and the SCR denitration system in sequence to become clean flue gas. The sintering (pelletizing) flue gas is subjected to a wet desulphurization system and a dust removal system to remove sulfur dioxide and dust, the temperature of the flue gas is reduced to 45-55 ℃, then the flue gas enters a carbon dioxide adsorption system, and carbon dioxide in the flue gas is adsorbed by a new complementary collector. And (4) the flue gas without carbon dioxide enters an SCR denitration system to remove nitrogen oxides, and the temperature of the flue gas is raised to about 110 ℃.
Through the structural design, the flue gas desulfurization, denitration, dust removal and decarburization system provided by the invention at least comprises the following beneficial effects: 1. all subsystems are organically structured, so that the desulfurization, denitration, dust removal and decarburization of the flue gas are realized; 2. through the structural design of the system, a small amount of denitrated clean flue gas can be extracted to desorb the complementary collecting agent which collects carbon dioxide, so that high-purity and high-concentration carbon dioxide gas is obtained for reuse, the effective utilization of waste gas waste heat can be realized, and the purposes of energy conservation, emission reduction and high-efficiency utilization of flue gas waste heat are achieved; 3. the original desulfurization, denitration and dust removal system of the flue gas is integrated with a newly-built carbon dioxide adsorption and desorption system, so that the one-time investment is saved, and the energy cost required in the desorption process is saved.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. Wherein:
FIG. 1 is a schematic diagram of the structure of a flue gas desulfurization, denitrification, dedusting and decarbonization system in an embodiment of the invention;
FIG. 2 is a schematic diagram of the configuration of a desulfurization subsystem in an embodiment of the present invention;
FIG. 3 is a schematic diagram of the denitration subsystem in the embodiment of the present invention;
FIG. 4 is a simplified schematic diagram of the configuration of the condensing subsystem in an embodiment of the present invention;
FIG. 5 is a schematic diagram of the dust removal subsystem in an embodiment of the present invention.
In fig. 1 to 5, the correspondence between the part names and the reference numerals is:
a desulfurization subsystem 1, a dust removal subsystem 2, a decarburization subsystem 3, a denitration subsystem 4,
A chimney 5, a carbon dioxide desorption subsystem 6 and a condensation subsystem 7;
a desulfurization absorption tower 11, an inlet flue 12 and a side outlet flue 13;
a rotary heat exchanger 41, a hot blast stove 42 and a denitration reactor 43;
Detailed Description
The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings. 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. It is therefore intended that the present invention encompass such modifications and variations as fall within the scope of the appended claims and equivalents thereof.
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" and "connected" used herein should be interpreted broadly, and may include, for example, a fixed connection or a detachable connection; they may be directly connected or indirectly connected through intermediate members, and specific meanings of the above terms will be understood by those skilled in the art as appropriate.
Referring to fig. 1 to 5, fig. 1 is a schematic structural diagram of a flue gas desulfurization, denitration, dedusting and decarbonization system according to an embodiment of the present invention; FIG. 2 is a schematic diagram of the configuration of a desulfurization subsystem in an embodiment of the present invention; FIG. 3 is a schematic diagram of the denitration subsystem in the embodiment of the present invention; FIG. 4 is a simplified schematic diagram of the configuration of the condensing subsystem in an embodiment of the present invention; FIG. 5 is a schematic diagram of the dust removal subsystem in an embodiment of the present invention.
The invention provides a flue gas desulfurization, denitration, dust removal and decarburization system which can be used for carrying out desulfurization, denitration (denitrification), dust removal and decarburization (removal of carbon dioxide) on flue gas, particularly sintering (pelletizing) flue gas.
In the invention, along the sequence of the flue gas treatment process, the flue gas desulfurization, denitration, dust removal and decarburization system comprises the following components in sequential connection: a desulfurization subsystem 1 for realizing the desulfurization of the flue gas (the first step is to carry out desulfurization treatment on the flue gas); a dust removal subsystem 2 for realizing the dust removal of the flue gas (the second step is to carry out dust removal treatment on the flue gas, and before dust removal, the invention can also add a flue gas cooling step); a decarbonization subsystem 3 for removing carbon dioxide from the flue gas (the third step is to decarbonize the flue gas, namely remove the carbon dioxide from the flue gas); and a denitration subsystem 4 for realizing the denitrification of the flue gas (the fourth step is to perform denitrification treatment on the flue gas). After the four flue gas treatment steps, high-temperature (110-130 ℃) clean flue gas can be obtained, for the clean flue gas, the invention has two treatment paths, namely two treated flue gas branches which are arranged in parallel are arranged, one treated flue gas branch is connected with a chimney 5 (used for directly discharging the flue gas) used for discharging the treated flue gas, the other treated flue gas branch is connected with a carbon dioxide desorption subsystem 6 (used for realizing the analysis treatment of the carbon dioxide capturing agent), and the carbon dioxide desorption subsystem 6 is in process connection with the decarburization subsystem 3 and is used for receiving the carbon dioxide capturing agent absorbed with carbon dioxide and carrying out carbon dioxide desorption operation on the carbon dioxide capturing agent.
Specifically, the temperature range of the flue gas output by the dedusting subsystem 2 is 40-55 ℃ (the lower the temperature is, the higher the removal rate of carbon dioxide in the flue gas is, under the premise that the temperature is not lower than 40 ℃), and the temperature range of the flue gas output by the denitration subsystem 4 is 110-130 ℃ (under the premise that no additional heating equipment is added, clean flue gas is used as a heat source).
Specifically, in the present invention, the desulfurization subsystem 1 is a wet desulfurization system. The desulfurization subsystem 1 comprises a pre-desulfurizer preparation subsystem for preparing a desulfurizer, a desulfurization tower connected with the pre-desulfurizer preparation subsystem for receiving the desulfurizer, and a desulfurization post-treatment subsystem. The flue gas is conveyed into a desulfurizing tower through a pipeline and is washed by a desulfurizing agent in the desulfurizing tower to be saturated flue gas, and the temperature of the flue gas is reduced from 120-180 ℃ to 50-60 ℃.
The saturated flue gas (and the unsaturated flue gas in the present application) refers to the water content in the flue gas, and the saturated flue gas at each temperature has a specific water content, and the saturated flue gas is saturated flue gas when the water content is reached, and the saturated flue gas is not unsaturated flue gas when the water content is reached.
Specifically, in the invention, the dust removal subsystem 2 is a wet-type electric dust remover, and the dust removal subsystem 2 can remove dust from the saturated flue gas at 50-60 ℃.
Further, a condensing subsystem 7 is arranged between the desulfurization subsystem 1 and the dust removal subsystem 2 and used for cooling the saturated flue gas at the temperature of 50-60 ℃, so that the requirement of the working temperature of the dust removal subsystem 2 is met. Specifically, the condensation subsystem 7 comprises a cooling tower, a condenser is arranged in the cooling tower, a circulating water tank is connected with the condenser, a circulating water pump is arranged on a cooling water circulating pipeline formed by the condenser and the circulating water tank, the flue gas exchanges heat with cooling water in the condenser, and the temperature is reduced from 50-60 ℃ to 40-55 ℃.
Specifically, in the invention, the decarbonization subsystem 3 comprises an adsorption tower, a capturing agent bed layer for dispersing a carbon dioxide capturing agent is arranged in the adsorption tower, a capturing agent inlet for inputting the carbon dioxide capturing agent, a capturing agent outlet for outputting the carbon dioxide capturing agent, flue gas inlet for inputting flue gas and a flue gas outlet for outputting the flue gas are arranged on the adsorption tower; the operating temperature range in the adsorption tower is 40-80 ℃.
Specifically, the decarbonization subsystem 3 is including the adsorption tower, and the shaft of adsorption tower is a tubular structure that has a take the altitude, and when using, the vertical setting of adsorption tower, the flue gas can upwards flow naturally like this, and the carbon dioxide trapping agent can rely on gravity to fall down naturally simultaneously for the flue gas stream produces the convection current with the carbon dioxide trapping agent stream (flue gas and carbon dioxide trapping agent are adverse current), improves the capture efficiency of carbon dioxide in the carbon dioxide trapping agent to the flue gas.
The carbon dioxide trapping agent is an organic high molecular polymer, the flue gas is mixed gas (after desulfurization and dust removal treatment, mainly contains carbon dioxide and oxynitride in the flue gas), the flue gas enters into the internal cavity space of the whole adsorption tower and can be filled, and the carbon dioxide trapping agent is required to be fully contacted with the flue gas in order to further improve the trapping efficiency of the carbon dioxide trapping agent on the carbon dioxide. In order to achieve the purpose, the invention is provided with a capturing agent bed layer for realizing the dispersion of the carbon dioxide capturing agent in the adsorption tower, and the carbon dioxide capturing agent is dispersed on a transverse layer (the adsorption tower is set to be vertical in the vertical direction and transverse in the horizontal direction in the use state, and the transverse layer is the transverse section of the adsorption tower) in the process of passing through the capturing agent bed layer, so that the carbon dioxide capturing agent is dispersed to the maximum extent. Of course, the invention can also increase the height of the adsorption tower properly, and increase the contact time of the carbon dioxide capturing agent and the flue gas by prolonging the falling path length of the carbon dioxide capturing agent, thereby achieving the purpose of improving the capturing efficiency of the carbon dioxide in the flue gas.
In one embodiment of the present invention, the main body of the adsorption tower is a cylindrical structure, the top of the main body is closed, and the lower end of the main body of the adsorption tower is provided with a funnel-shaped structure, so that the carbon dioxide capturing agent (the carbon dioxide capturing agent with carbon dioxide adsorbed thereon) can be gathered and output (without residue) for analysis. The shape of the main body of the adsorption column may be circular in cross section (i.e., the cylindrical structure described above), or may be rectangular, elliptical, or regular polygonal.
Because the flue gas and the carbon dioxide trapping agent are required to be input into the adsorption tower for adsorbing and removing the carbon dioxide, the adsorption tower is provided with a trapping agent inlet for inputting the carbon dioxide trapping agent, a trapping agent outlet for outputting the carbon dioxide trapping agent, flue gas inlet for inputting the flue gas and a flue gas outlet for outputting the flue gas. Specifically, a trapping agent inlet is arranged at the top of the adsorption tower, a trapping agent outlet is arranged at the bottom of the adsorption tower, a flue gas outlet is arranged on the side wall of the adsorption tower and close to the top of the adsorption tower, and a flue gas inlet is arranged on the side wall of the adsorption tower and close to the bottom of the adsorption tower. Through the layout arrangement of the inlet and the outlet, the carbon dioxide trapping agent and the flue gas form countercurrent inside the adsorption tower.
The working temperature range of the carbon dioxide collector for adsorbing carbon dioxide is 40-80 ℃, so the operating temperature range in the adsorption tower is set to be 40-80 ℃.
The trapping agent bed layer arranged in the adsorption tower has the following specific structure: the collecting agent bed layer comprises a plurality of dispersing units which are transversely arranged, each dispersing unit comprises a unit main body in the shape of a cylinder with the same diameter, conical structures are arranged at two ends of each unit main body, the dispersing units are integrally in a fusiform structure, and when the dispersing units are arranged, the unit main bodies are provided with certain gaps and form adsorption gaps which are beneficial to the passing of flue gas and carbon dioxide collecting agents, so that the carbon dioxide collecting agents can be dispersed and uniformly mixed with the flue gas through the collecting agent bed layer, and the aim of improving the adsorption efficiency of the carbon dioxide in the flue gas is fulfilled.
Specifically, in the invention, the carbon dioxide desorption subsystem 6 comprises an analysis tower, the analysis tower is provided with an analysis inlet and an analysis outlet, the direction of the analysis inlet pointing to the analysis outlet is the analysis direction, an analysis path is formed in the analysis tower and along the analysis direction, the analysis path comprises an analysis section, and the operating temperature range of the analysis section is 110-130 ℃.
The carbon dioxide in the waste gas can be effectively absorbed and removed through the carbon dioxide trapping agent, and in order to reduce the operation cost, the invention also provides a carbon dioxide desorption subsystem 6 to realize the cyclic utilization of the carbon dioxide trapping agent.
Specifically, the carbon dioxide desorption subsystem 6 includes an analytical tower, the analytical tower has a shape similar to that of the adsorption tower, the main body part of the analytical tower is an equal-diameter cylindrical structure (cylinder), the top of the analytical tower is closed, the bottom of the analytical tower is provided with a funnel-shaped structure, and the carbon dioxide trapping agent adsorbed with carbon dioxide is input from the top of the analytical tower, is heated, analyzed and cooled, and is output from the bottom of the analytical tower.
From the above, the working temperature of the carbon dioxide capturing agent during carbon dioxide adsorption is between 40 ℃ and 80 ℃, and the temperature of the carbon dioxide capturing agent during analysis is between 110 ℃ and 130 ℃, so that the carbon dioxide can be analyzed only by heating the carbon dioxide capturing agent to 110 ℃ to 130 ℃ after entering the inside of the analysis tower, the temperature of the carbon dioxide capturing agent after analysis is high, and the carbon dioxide can be rapidly entered into the adsorption tower for carbon dioxide adsorption only by cooling, therefore, the inside of the analysis tower needs to be heated and analyzed and cooled for the carbon dioxide capturing agent. Specifically, the analysis tower is provided with an analysis inlet and an analysis outlet, the direction of the analysis inlet pointing to the analysis outlet is the analysis direction, an analysis path is formed in the analysis tower along the analysis direction, the analysis path comprises an analysis section, and the operating temperature range of the analysis section is 110-130 ℃. Along the analytic direction, the analytic route is located the low reaches of analytic section and still is provided with the cooling zone, corresponds the cooling zone, is provided with cooling structure in the analytic tower. In an actual use state, the analytic tower is vertically arranged (has a certain height), the analytic inlet is arranged at the top of the analytic tower, and the analytic outlet is arranged at the bottom of the analytic tower. The upper part of the middle part of the desorption tower is used for heating up and desorbing the carbon dioxide trapping agent, and the lower part of the middle part of the desorption tower is used for cooling down the carbon dioxide trapping agent.
The analytic inlet is arranged at the top of the analytic tower, the analytic outlet is arranged at the bottom of the analytic tower, the analytic inlet is connected with the trapping agent outlet through a conveying system, the carbon dioxide trapping agent can be conveyed into the analytic tower through the conveying system after adsorbing carbon dioxide, the analytic outlet is in butt joint with the trapping agent inlet, and the conveying system can be arranged between the analytic outlet and the trapping agent inlet and used for conveying the carbon dioxide trapping agent after analysis, so that the carbon dioxide trapping agent can be recycled. In the present invention, the conveying system is a conveying system capable of conveying particulate material, such as a belt conveying system or a bucket conveyor.
The side wall of the desorption tower and the lower end corresponding to the desorption section are provided with a desorption gas source inlet (used for inputting high-temperature desorption gas), and the side wall of the desorption tower and the upper end corresponding to the desorption section are provided with a desorption gas rich gas outlet (used for outputting carbon dioxide rich gas).
Specifically, in the present invention, the denitration subsystem 4 is an SCR denitration system.
Therefore, the flue gas desulfurization, denitration, dust removal and decarburization system provided by the invention comprises a plurality of subsystems and is used for realizing desulfurization, denitration, dust removal and decarburization of flue gas.
In the invention, a desulfurization subsystem 1 comprises a desulfurization absorption tower 11, flue gas enters the tower from an inlet flue 12 of the desulfurization absorption tower 11 obliquely downwards, the flue gas sequentially passes through a spraying layer, a high-efficiency desulfurization unit and a demister from bottom to top, the flue gas and desulfurization slurry reversely contact (the flow direction of the flue gas is opposite to that of the desulfurization slurry to form a reverse flow) in the spraying section (the spraying layer) and the high-efficiency desulfurization section (the high-efficiency desulfurization unit), the slurry sprayed by the spraying layer treats the flue gas, the flue gas is cooled, dust is condensed, and sulfur dioxide is purified. The purified flue gas is subjected to mist drop removal in a demister section and is discharged from an exhaust flue 13 on the side of the absorption tower. For the condensing subsystem 7, the condensing subsystem 7 mainly comprises a condenser 71, a cooling tower 72, a cooling water circulating pump and a condensate treatment device matched with the cooling water circulating pump, the condenser 71 is installed between the desulfurization absorption tower 11 and the wet electric dust collector, saturated flue gas (saturated flue gas means that moisture in the flue gas reaches a saturated state) output from the outlet of the desulfurization absorption tower 11 enters the condenser 71 to exchange heat with cold water conveyed by the cooling water circulating pump, so that the temperature of the flue gas is reduced, and precipitated condensate is recycled. The cold water after heat exchange is heated and returns to the cooling tower 72 for cooling. The cooling tower 72 cools the hot water using fans and packing (make-up cold water). For the dust removal subsystem 2, the dust removal subsystem 2 mainly includes a wet electric dust remover and a flue demister. Liquid drops and dust particles in the smoke are split and further atomized after being charged in a strong corona field formed by the bur electrode, electric field force and charged water mist collide, intercept, adsorb and condense, the dust particles are captured together, and finally the dust particles reach a dust collecting electrode under the driving of the electric field force and are captured. And the flue demister collects and removes liquid drops generated when the wet-type electric dust collector is washed. For the denitration subsystem 4, the denitration subsystem 4 mainly includes a rotary heat exchanger 41, a hot blast stove 42, a denitration reactor 43 and a reducing agent preparation and injection system. The dedusted flue gas enters a rotary heat exchanger 41 for heating, a hot blast stove 42 burns fuel (blast furnace gas, converter gas, coke oven gas and the like) to heat the flue gas again, and the flue gas enters an SCR reactor to remove nitrogen oxides after reaching the reaction temperature of the denitration catalyst. The denitrated clean flue gas enters the rotary heat exchanger 41 again to heat the original flue gas, and the cooled flue gas is discharged to the chimney 5.
The invention provides a flue gas treatment system for desulfurization, denitration, dust removal and decarburization of sintering (pelletizing) flue gas, which comprises a wet desulfurization system (a desulfurization subsystem 1), a dust removal system (comprising a dust removal subsystem 2 and a condensation subsystem 7), an SCR denitration system (a denitration subsystem 4) and a dry adsorption carbon dioxide removal system (a decarburization subsystem 3 and a carbon dioxide desorption subsystem 6). The subsystems are mutually influenced and connected, the flue gas is processed by the wet desulphurization system, the dedusting system, the carbon dioxide adsorption system and the SCR denitration system in sequence to become clean flue gas (the flue gas temperature is 110-130 ℃), and the extracted hot flue gas (clean flue gas) after partial denitration enters the carbon dioxide desorption subsystem 6 to desorb the carbon dioxide for the carbon dioxide trapping agent adsorbed with the carbon dioxide. The sintering (pelletizing) flue gas is subjected to a wet desulphurization system and a dust removal system to remove sulfur dioxide and dust, the temperature of the flue gas is reduced to 45-55 ℃, then the flue gas enters a carbon dioxide adsorption system, and carbon dioxide in the flue gas is adsorbed by a new complementary collector. And (3) introducing the flue gas subjected to carbon dioxide removal into an SCR denitration system to remove nitrogen oxides, and heating the flue gas to about 110 ℃. And extracting a small amount of denitrated clean flue gas to desorb the complementary collecting agent which collects the carbon dioxide, so as to obtain high-purity and high-concentration carbon dioxide gas for recycling. The original desulfurization, denitration and dust removal system of the flue gas is integrated with a newly-built carbon dioxide adsorption and desorption system, so that the one-time investment is saved, and the energy cost required in the desorption process is saved.
The flue gas treatment process of the invention is briefly described as follows: 1. the sintering (pelletizing) flue gas enters a wet desulphurization system firstly, the wet desulphurization system mainly comprises a desulphurization tower, a pre-desulfurizer preparation subsystem and a post-desulphurization treatment subsystem, the flue gas is washed by a desulfurizer in the desulphurization tower to be saturated flue gas, and the temperature is reduced from 120-180 ℃ to 50-60 ℃; 2. the saturated flue gas enters a condenser for cooling, a condensing system mainly comprises the condenser, a cooling tower, a circulating water tank and a circulating water pump, the flue gas exchanges heat with cooling water in the condenser, and the temperature is reduced from 50-60 ℃ to 40-55 ℃; 3. the flue gas enters a wet-type electric dust collector to remove particles, and the concentration of the particles is less than 10mg/Nm 3 The temperature of the flue gas is slightly reduced; 4. the low-temperature flue gas enters a carbon dioxide adsorption tower, the operation temperature is 40-80 ℃, the lower the temperature is, the more carbon dioxide is favorably adsorbed, a carbon dioxide adsorption system mainly comprises an adsorption tower and a carbon dioxide complementary agent storage and conveying system, and the adsorption tower is in a counter-current fluidized bed type; 5. the flue gas of desorption carbon dioxide gets into SCR reactor desorption nitrogen oxide, and SCR deNOx systems mainly includes SCR reactor, heating furnace heating system, GGH heat transfer device.
The flue gas discharged from the SCR reactor is clean flue gas for removing sulfides, carbon dioxide, particulate matters and nitrogen oxides, the temperature is 110-130 ℃ (after the draught fan is pressurized and heated), a small amount of clean flue gas is extracted and enters a carbon dioxide desorption system, and the rest of clean flue gas is discharged through a chimney 5. The carbon dioxide desorption system mainly comprises a desorption tower, a carbon dioxide complementary agent preheater and a carbon dioxide complementary agent cooler.
The invention adds the flue gas decarbonization device in the existing sintering (pelletizing) flue gas treatment process, does not change the operation parameters of the original flue gas desulfurization, denitration and dust removal device, and the decarbonization device is integrated into the whole flue gas treatment process. Meanwhile, the purified flue gas (flue gas subjected to desulfurization, denitration, dust removal and decarburization) is used as the analysis gas to desorb the complementary collector trapping the carbon dioxide, so that the carbon dioxide gas with high purity and high concentration is obtained for recycling, other energy sources are not used for analyzing the complementary collector, and the operation cost is saved. The whole system has high fusion degree and saves one-time investment. The flue gas treatment system (flow) is a necessary choice for decarburization treatment of sintering (pelletizing) flue gas.
Specifically, the carbon dioxide collecting agent used in the invention is an organic carbon dioxide collecting agent with the pore diameter ranging from 15nm to 25 nm.
The above 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 to the present invention 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 (10)
1. The utility model provides a flue gas desulfurization, denitration, dust removal and decarbonization system which characterized in that, along flue gas treatment process order, flue gas desulfurization, denitration, dust removal and decarbonization system are including connecting gradually:
a desulfurization subsystem (1) for implementing flue gas desulfurization;
a dust removal subsystem (2) for realizing the dust removal of the flue gas;
a decarbonization subsystem (3) for removing carbon dioxide from the flue gas;
a denitration subsystem (4) for realizing the denitrification of the flue gas;
the system comprises a decarbonization subsystem, a chimney exhaust system and two treated flue gas branches, wherein one treated flue gas branch is connected with the chimney (5) used for exhausting treated flue gas, the other treated flue gas branch is connected with the carbon dioxide desorption subsystem (6), and the carbon dioxide desorption subsystem is connected with the decarbonization subsystem in a process manner and is used for receiving a carbon dioxide trapping agent adsorbed with carbon dioxide and carrying out carbon dioxide desorption operation on the carbon dioxide trapping agent;
wherein the temperature range of the flue gas output by the dedusting subsystem is 40-55 ℃, and the temperature range of the flue gas output by the denitration subsystem is 110-130 ℃.
2. The flue gas desulfurization, denitrification, dedusting and decarbonization system of claim 1,
the desulfurization subsystem is a wet desulfurization system;
the desulfurization subsystem comprises a pre-desulfurizer preparation subsystem for preparing a desulfurizer, a desulfurization tower connected with the pre-desulfurizer preparation subsystem for receiving the desulfurizer and a desulfurization post-treatment subsystem;
the flue gas is washed by a desulfurizer in the desulfurizing tower to be saturated flue gas, and the temperature is reduced from 120-180 ℃ to 50-60 ℃.
3. The flue gas desulfurization, denitrification, dedusting and decarbonization system of claim 1,
the dust removal subsystem is a wet-type electric dust remover.
4. The flue gas desulfurization, denitrification, dedusting and decarbonization system of claim 3,
a condensing subsystem (7) is also arranged between the desulfurization subsystem and the dedusting subsystem;
the condensation subsystem comprises a cooling tower, a condenser is arranged in the cooling tower, a circulating water pool is connected with the condenser, and a circulating water pump is arranged on a cooling water circulating pipeline formed by the condenser and the circulating water pool;
the flue gas is changed into saturated flue gas by heat exchange with cooling water in the condenser, and the temperature is reduced from 50-60 ℃ to 40-55 ℃.
5. The flue gas desulfurization, denitrification, dedusting and decarbonization system of claim 1,
the decarbonization subsystem comprises an adsorption tower, a capturing agent bed layer used for dispersing a carbon dioxide capturing agent is arranged in the adsorption tower, a capturing agent inlet used for inputting the carbon dioxide capturing agent, a capturing agent outlet used for outputting the carbon dioxide capturing agent, flue gas inlet used for inputting flue gas and a flue gas outlet used for outputting the flue gas are arranged on the adsorption tower.
6. The flue gas desulfurization, denitrification, dedusting and decarbonization system of claim 5,
the carbon dioxide desorption subsystem comprises an analysis tower, an analysis inlet and an analysis outlet are arranged on the analysis tower, the direction of the analysis inlet pointing to the analysis outlet is an analysis direction, an analysis path is formed in the analysis tower and along the analysis direction, and the analysis path comprises an analysis section.
7. The flue gas desulfurization, denitrification, dedusting and decarbonization system of claim 6,
the operating temperature range in the adsorption tower is 40-80 ℃;
the operating temperature range of the resolving section is 110-130 ℃.
8. The flue gas desulfurization, denitrification, dedusting and decarbonization system of claim 7,
the top of the adsorption tower is provided with the trapping agent inlet, the bottom of the adsorption tower is provided with the trapping agent outlet, the side wall of the adsorption tower and the position close to the top of the adsorption tower are provided with the flue gas outlet, and the side wall of the adsorption tower and the position close to the bottom of the adsorption tower are provided with the flue gas inlet;
and the carbon dioxide trapping agent and the flue gas form countercurrent in the adsorption tower.
9. The flue gas desulfurization, denitrification, dedusting and decarbonization system of claim 8,
the analysis inlet is arranged at the top of the analysis tower, the analysis outlet is arranged at the bottom of the analysis tower, the analysis inlet is connected with the collector agent outlet through a conveying system, and the analysis outlet is in butt joint with the collector agent inlet and is used for realizing the recycling of the carbon dioxide collector agent;
and a desorption gas source inlet is formed in the side wall of the desorption tower and corresponds to the lower end of the desorption section, and a desorption gas rich gas outlet is formed in the side wall of the desorption tower and corresponds to the upper end of the desorption section.
10. The flue gas desulfurization, denitrification, dedusting and decarbonization system of claim 1,
the denitration subsystem is an SCR denitration system.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116764381A (en) * | 2023-06-14 | 2023-09-19 | 临涣焦化股份有限公司 | CO trapping device for coke oven flue gas 2 Apparatus and method of (a) |
| US12083472B1 (en) * | 2023-07-07 | 2024-09-10 | Shanxi Dadi Ecological Environment Technology Research Institute Co., Ltd. | Device and method for capturing carbon dioxide and producing organic weak acid salt |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116764381A (en) * | 2023-06-14 | 2023-09-19 | 临涣焦化股份有限公司 | CO trapping device for coke oven flue gas 2 Apparatus and method of (a) |
| CN116764381B (en) * | 2023-06-14 | 2024-01-23 | 临涣焦化股份有限公司 | CO trapping device for coke oven flue gas 2 Apparatus and method of (a) |
| US12083472B1 (en) * | 2023-07-07 | 2024-09-10 | Shanxi Dadi Ecological Environment Technology Research Institute Co., Ltd. | Device and method for capturing carbon dioxide and producing organic weak acid salt |
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