CN212999279U - Flue gas treatment system for efficiently utilizing carbon monoxide - Google Patents
Flue gas treatment system for efficiently utilizing carbon monoxide Download PDFInfo
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Abstract
The utility model discloses a flue gas processing system that carbon monoxide high efficiency utilized, this system including desulphurization unit, dust collector, flue gas diverging device, catalytic oxidation device, flue gas mixed flow device and catalytic reduction device. The utility model converts a part of carbon monoxide in the flue gas after desulfurization and dust removal into carbon dioxide by catalytic oxidation, and then converts the carbon dioxide into the carbon dioxide by the catalytic oxidation with the rest partThe flue gas mixes and carries out CO catalytic reduction denitration, and the heat that carbon monoxide catalytic oxidation process was earlier given off directly is used for the denitration process simultaneously, has reduced or even avoided the process of heating up the flue gas through external fuel heating, has practiced thrift the energy and has also replaced traditional SCR denitration process reductant NH simultaneously3The use of (1). The waste is treated by waste, and the pollution of the smoke to the environment is reduced.
Description
Technical Field
The utility model relates to a flue gas processing technology, concretely relates to flue gas processing system of high-efficient utilization of carbon monoxide belongs to flue gas purification technical field.
Background
Particulate matter, sulfur oxides, nitrogen oxides are one of the major sources of air pollution. For industrial flue gas, especially for sintering machine flue gas in the steel industry, flue gas dust removal, desulfurization and denitration technology is an important means for reducing emission of particulate matters, nitrogen oxides and sulfur oxides.
The flue gas dedusting refers to the purpose of separating dust in flue gas through a deduster so as to purify the flue gas or recover materials. The dust removal methods adopted in the industry at present mainly comprise a mechanical dust removal technology, a wet dust removal technology, an electrostatic dust removal technology and a bag type dust removal technology. The mechanical dust removal technology is used for separating dust by utilizing the gravity settling, inertia or centrifugal force of the dust, the dust removal efficiency is generally below 90 percent, the dust removal efficiency is low, the resistance is low, and the mechanical dust removal technology has the advantages of energy conservation; the wet dust removal technology is to separate dust in a dust-containing gas into liquid by utilizing a gas-liquid contact washing principle so as to remove the dust in the gas. The dust removal efficiency is slightly higher than that of a mechanical dust remover, but the secondary pollution of washing liquid is easily caused; the electrostatic dust removal technology is that dust particles are charged by passing dust-containing gas through a strong electric field, and when the dust-containing gas passes through a dust removal electrode, particles with positive/negative charges are respectively adsorbed by a negative/positive electrode plate, so that dust in the gas is removed; the bag type dust removal technology is that a fiber filter material is used for collecting solid particles in dust-containing gas to form a filter dust cake, and fine dust particles are further filtered through the filter dust cake, so that the purpose of high-efficiency dust removal is achieved.
Flue gas desulfurization refers to the removal of Sulfur Oxides (SO) from flue gas or other industrial waste gases2And SO3). Eyes of a userThe desulfurization methods previously used in industry include dry desulfurization, semi-dry desulfurization or wet desulfurization. Compared with the conventional wet scrubbing process, the dry flue gas desulfurization process has the following advantages: the investment cost is low; the desulfurization product is in a dry state and is mixed with fly ash; a demister and a reheater are not required to be arranged; the equipment is not easy to corrode and scale formation and blockage are not easy to occur. The semidry desulfurization mainly adopts the atomized lime slurry to contact with flue gas in a spray drying tower, and the lime slurry and SO2After the reaction, a dry solid reactant is generated and finally collected by a dust remover together with fly ash. The wet desulfurization mainly uses limestone, lime or sodium carbonate and other slurry as a washing agent to wash the flue gas in a reaction tower SO as to remove SO in the flue gas2Its main advantages are high desulfurizing efficiency, high synchronous running rate, rich resources of absorbent, and high commercial value.
Denitration of flue gas means reduction of NOx generated to N2So as to remove NOx in the flue gas, the denitration method adopted by the industry at present mainly comprises a Selective Catalytic Reduction (SCR) method and a selective non-catalytic reduction (SNCR) method. The SCR denitration is that under the condition of catalyst existence, ammonia, urea and the like are used as reducing agents, NO in the flue gas is reduced into N under the condition of oxygen existence and certain temperature2. SNCR is a mature low-cost denitration technology, which takes a hearth or a predecomposition furnace in the cement industry as a reactor, sprays reducing agent containing amino into the hearth, and the reducing agent reacts with NOx in flue gas to generate N2And H2O。
In the prior art, most of the treatment aiming at the flue gas adopts a combined process of dust removal, desulfurization and denitration. Generally, the temperature for dry desulfurization is generally controlled within the range of 100-150 ℃, the temperature for semi-dry desulfurization is generally controlled within the range of 90-110 ℃, and the temperature for wet desulfurization is generally controlled within the range of 50-60 ℃. Then entering a denitration process, and adopting a Selective Catalytic Reduction (SCR) method for denitration, wherein the temperature is generally controlled to be about 150 ℃ and 400 ℃; if the selective non-catalytic reduction SNCR method is adopted for denitration, the temperature is controlled to be between 800 and 1100 ℃ in general. In the prior art, the temperature of the flue gas to be treated is preferentially adjustedSaving the temperature range suitable for desulfurization treatment, generally lowering the temperature, then heating the desulfurized flue gas to raise the temperature of the desulfurized flue gas to the temperature range suitable for denitration. In the process, because the amount of the flue gas to be treated is large, a large amount of fuel is consumed for heating the flue gas after desulfurization treatment; in addition, the SCR denitration reaction process needs to consume a large amount of NH3The potential safety hazard is high in the using process, and the ammonia escapes to cause resource waste and secondary environmental pollution; meanwhile, most SCR catalysts are vanadium-titanium systems, have high biological toxicity and great threat to the ecological environment, and are difficult to regenerate after being poisoned.
In addition, because the flue gas to be treated is generated by the combustion of fuel, the flue gas contains a certain amount of carbon monoxide because the combustion is sufficient and the fuel cannot be completely and fully combusted. In the prior art, the national emission standard of carbon monoxide is not specifically specified at present, so that the flue gas to be treated is directly discharged after being subjected to desulfurization and denitrification treatment, and the carbon monoxide in the flue gas is not specifically treated and utilized, so that the carbon monoxide is directly discharged. Meanwhile, carbon monoxide is colorless, odorless and nonirritating gas; the solubility in water is very low, and the water is extremely insoluble; the explosion limit of the mixture with air is 12.5-74.2%. Carbon monoxide is easily combined with hemoglobin to form carboxyhemoglobin, so that the hemoglobin loses the oxygen carrying capacity and function, and the tissues are suffocated and die in serious cases. Carbon monoxide has toxic effects on systemic histiocytes, and especially on the cerebral cortex. Therefore, the direct emission of carbon monoxide has great environmental pollution, and the positive significance of reducing and even avoiding the emission of CO.
Chinese patent CN108568207A discloses an efficient and energy-saving sintering flue gas multi-pollutant purification process, which carries out SCR denitration after CO catalytic oxidation removal on desulfurized flue gas. Similarly, Chinese patent CN108579369A discloses a system and a method for the cooperative treatment of multiple pollutants in coke oven flue gas by CO catalysisAnd (3) coupling oxidation and SCR denitration to realize CO removal and NOx removal. Chinese patent CN108692579A "a CO-processing technology of sinter waste heat and sintering flue gas pollutants" discloses a CO-processing technology of sinter waste heat and sintering flue gas pollutants, which removes CO in flue gas through two steps of heat exchange processing and decarbonization processing, and then removes nitrogen oxides in the flue gas through SCR denitration processing. The above patents can realize the resource utilization of CO removal and the supply of reaction heat to SCR denitration. But does not address the SCR denitration process NH3The use of the vanadium-titanium catalyst and the use of the vanadium-titanium catalyst.
SUMMERY OF THE UTILITY MODEL
To prior art not enough, the utility model provides a flue gas processing system that carbon monoxide high efficiency was utilized, through utilizing the carbon monoxide in the flue gas, turn into carbon dioxide with some carbon monoxide catalytic oxidation in the desulfurization dust removal back flue gas, the heat that this process was emitted directly is used for the denitration process of remainder carbon monoxide catalytic NOx reduction, reduced the process of having avoided heating up the flue gas through external fuel even, practiced thrift the energy and also replaced traditional SCR denitration process reductant NH simultaneously3The use of (1). The utility model makes full use of the carbon monoxide in the flue gas, on one hand, the heat emitted in the process of converting carbon dioxide by catalytic oxidation of carbon monoxide is used by the subsequent process, thereby saving or even saving the use of fuel; on the other hand, carbon monoxide is used for catalyzing NOx reduction and replaces a reducing agent NH in the traditional SCR denitration process3The carbon monoxide in the flue gas is treated simultaneously, the waste is treated by the waste, and the pollution of the flue gas to the environment is reduced.
In order to achieve the above object, the utility model discloses the technical scheme who adopts specifically as follows:
according to the utility model discloses a first embodiment provides a flue gas processing system that carbon monoxide high efficiency utilized, and this system is including desulphurization unit, dust collector, flue gas diverging device, catalytic oxidation device, flue gas mixed flow device and catalytic reduction device. The original flue gas conveying pipeline is communicated to the desulfurization device. And the desulfurization device is communicated to the dust removal device through a second pipeline. And the dust removal device is communicated to the flue gas flow dividing device through a third pipeline. And a fourth pipeline is branched from the flue gas flow dividing device and communicated to the catalytic oxidation device. And a fifth pipeline is also branched from the flue gas flow dividing device and communicated to the flue gas flow mixing device. And a sixth pipeline is divided from the reduction and oxidation device and communicated to a fifth pipeline (which is conveyed to the flue gas mixed flow device through the fifth pipeline). And the flue gas flow mixing device is communicated to the catalytic reduction device through a seventh pipeline. The catalytic reduction device is communicated to the outside through an eighth pipeline.
Preferably, the system further comprises a heat supplementing device. The heat supplementing device is arranged on the fourth pipeline.
Preferably, the system further comprises an oxygen supply device. The oxygen supplementing device is connected with the catalytic oxidation device through an oxygen delivery pipeline.
Preferably, the system further comprises a heat exchange device. The heat exchange device is arranged on the seventh pipeline.
Preferably, the system also comprises a waste heat recovery device. The waste heat recovery device is arranged on the eighth pipeline.
Preferably, the system further comprises a first flow detection device. The first flow detection device is arranged on the third pipeline.
Preferably, the system further comprises a second flow detection device. The second flow detection device is arranged on the fourth pipeline.
Preferably, the system further comprises a first valve. The first valve is arranged on the fourth pipeline.
Preferably, the system further comprises a second valve. The second valve is disposed on the fifth conduit.
Preferably, the system further includes a CO concentration detection device, a NOx concentration detection device, an oxygen concentration detection device, and a temperature detection device. And the CO concentration detection device, the NOx concentration detection device, the oxygen concentration detection device and the temperature detection device T are all arranged in the smoke diversion device.
According to the second embodiment of the present invention, there is provided a flue gas treatment method for efficiently utilizing carbon monoxide or a flue gas treatment system for efficiently utilizing carbon monoxide according to the first embodiment, the method comprises the following steps:
1) the raw flue gas is conveyed to a desulfurization device through a first pipeline for desulfurization treatment, and the desulfurized flue gas is conveyed to a dust removal device through a second pipeline for dust removal treatment. And then conveying the desulfurized and dedusted flue gas to a flue gas shunting device through a third pipeline for flue gas shunting treatment.
2) After part of the desulfurized and dedusted flue gas in the flue gas flow dividing device is subjected to heat supplement by the heat supplementing device or not, the desulfurized and dedusted flue gas is conveyed to the catalytic oxidation device through the third pipeline L3 to be subjected to CO catalytic oxidation treatment when the oxygen supplementing device is started or not started, and the part of the flue gas subjected to CO catalytic oxidation treatment is conveyed to the flue gas flow mixing device through the sixth pipeline to be subjected to flue gas flow mixing treatment. Meanwhile, the residual flue gas in the flue gas flow distribution device after desulfurization and dust removal is directly conveyed into the flue gas flow mixing device through a fifth pipeline for flue gas flow mixing treatment.
3) And the mixed flue gas after the flue gas mixed flow treatment is finished by the flue gas mixed flow device is conveyed into the catalytic reduction device by a seventh pipeline for NOx catalytic reduction treatment after or without heat exchange of the heat exchange device. And the clean flue gas after the NOx catalytic reduction treatment is discharged through an eighth pipeline after the waste heat of the waste heat recovery device is recovered.
Preferably, the method also comprises the step of arranging a first flow detection device on the third pipeline to detect the flow of the flue gas subjected to desulfurization and dust removal in real time as v1 and Nm3H is used as the reference value. A second flow detection device is arranged on the fourth pipeline for detecting the flow of the desulfurized and dedusted flue gas distributed to the catalytic oxidation device in real time as v2, Nm3H is used as the reference value. A CO concentration detection device is also arranged in the flue gas flow distribution device for detecting the volume concentration of CO in the flue gas after desulfurization and dust removal to be p1, ppm/Nm3. A NOx concentration detection device is also arranged in the flue gas flow dividing device for detecting the volume concentration r1, ppm/Nm of NOx in the flue gas after desulfurization and dust removal in real time3. The fourth pipeline is also provided with a first valve, and the fifth pipeline is also provided with a second valve. Then:
v2 × p1 (1-b) + (v1-v2) × p1 ═ a × v1 × r1.
In the formula I, a is a CO surplus coefficient of the content of CO in the catalytic reduction device relative to the content of NOx, and the value is 1-2, preferably 1.1-1.8, and more preferably 1.3-1.5. And b is the CO combustion coefficient in the catalytic oxidation device, and the value is 0.1-1, preferably 0.4-0.95, and more preferably 0.7-0.9.
Formula I is converted to:
formula II, (v1-a v1 r1/p1)/b.
The flow of the desulfurized and dedusted flue gas which is distributed and conveyed to the catalytic oxidation device through the fourth pipeline is calculated as the value v2, Nm of the formula II by regulating and controlling the first valve3/h。
Preferably, the method also comprises the step of arranging an oxygen concentration detection device in the flue gas flow dividing device to detect the volume concentration of oxygen in the flue gas subjected to desulfurization and dust removal to be s1, ppm/Nm3. The catalytic oxidation device is also connected with the oxygen supply device through an oxygen pipeline. The oxygen excess coefficient in the catalytic oxidation device is set as c, and the value is 1-2, preferably 1.1-1.8, and more preferably 1.3-1.5. Then:
preferably, s1 is 0.5 × p1 × b × c. The oxygen content is sufficient and the system is not treated.
Preferably, when s1 < 0.5 × p1 × b × c. And (3) starting an oxygen supplementing device to supplement oxygen-containing gas into the catalytic oxidation device when the oxygen content is insufficient, wherein the oxygen supplementing quantity is N, ppm:
N＝0.5*v2*p1*b*c-v2*s1.., formula III.
When the oxygen content in the catalytic oxidation device is insufficient, the oxygen supplementing quantity conveyed to the catalytic oxidation device through the oxygen conveying pipeline by the oxygen supplementing device is regulated and controlled to be the calculated value N, ppm of the formula III.
Preferably, the method also comprises the step of arranging a temperature detection device in the flue gas diversion device to detect the temperature t1 and DEG C of the flue gas subjected to desulfurization and dust removal in real time. The CO catalytic oxidation activation temperature in the catalytic oxidation device is set to t2 and DEG C. Then:
preferably, when t1 ≧ t2, the system does not process.
Preferably, when t1 is less than t2, the heat supplementing device is started to supplement heat to the desulfurized and dedusted flue gas conveyed to the catalytic oxidation device, and the heat supplementing quantity is Q1, kJ:
q1 ═ C × v2. (t2-t 1).
In the formula IV, C is the average specific heat capacity of the flue gas after desulfurization and dust removal, and kJ/DEG C.g. The heat quantity for supplementing heat to the desulfurized and dedusted flue gas conveyed to the catalytic oxidation device by starting the heat supplementing device is calculated value Q1, kJ of formula IV.
Preferably, the method further comprises providing a heat exchange device on the seventh conduit. Setting the heat production quantity of CO catalytic oxidation in the catalytic oxidation device to be Q2kJ. The temperature of the mixed flue gas in the flow mixing device is set to be t3 and DEG C. Setting the activation temperature of CO catalytic reduction NOx in the catalytic reduction device to t4At deg.C. Then:
Q2＝b*v2*p1*28/22.4*10-3formula V28 x 283.
t3 ═ t1+ k (Q1+ Q2)/(C × v1).
Substituting formula IV and formula V into formula VI to obtain:
t3＝t1+[k*(t2-t1)*C*v2+k*b*v2*p1*28/22.4*10-3/28*283]v1.
Wherein k is a heat transfer coefficient, and is 0.7-1, preferably 0.8-0.98, and more preferably 0.9-0.95. The heat of combustion of CO was 283 kJ/mol. The relative molecular mass of CO was 28. The volume of any gas of 1mol under standard conditions is 22.4L.
Preferably, when t3 is t4, the system does not process.
Preferably, when t3 < t4, the heat exchange device is started to heat the mixed flue gas conveyed to the flow mixing device, and the heating heat is Q3, kJ:
q3 ═ C ═ v1.. formula VIII (t4-t 3).
The heat quantity for heating the mixed flue gas conveyed into the flow mixing device by starting the heat exchange device is the calculated value Q3, kJ of the formula VIII.
Preferably, when t3 is greater than t4, the heat exchange device is started or not started (in practical cases, the temperature at the position is not much higher than the actually required temperature, and optionally, the temperature is not reduced), and the heat absorption treatment is carried out on the mixed flue gas conveyed into the flow mixing device, wherein the heat absorption heat is Q4, kJ:
q4 ═ C ═ v1.. formula IX (t3-t 4).
The heat quantity absorbed by the mixed flue gas conveyed into the flow mixing device by starting the heat exchange device is calculated value Q4, kJ of formula IX.
Preferably, the method further comprises the step of arranging a waste heat recovery device on the eighth pipeline to recycle heat in the clean flue gas.
Preferably, the waste heat in the clean flue gas absorbed by the waste heat recovery device is used for the heat supplementing device or the heat exchanging device.
In the prior art, since the flue gas to be treated is generated by the combustion of fuel, and because the combustion is sufficient and the fuel cannot be completely and sufficiently combusted, the flue gas not only contains a large amount of NOx but also contains CO at a high concentration (6000 mg/Nm)3Left and right), although the national emission standard of carbon monoxide is not clearly specified at present, the flue gas to be treated is generally directly discharged only after being subjected to desulfurization and denitrification treatment, and the carbon monoxide in the flue gas is not specifically treated and utilized, so that the carbon monoxide is directly discharged. Meanwhile, carbon monoxide is colorless, odorless and nonirritating gas; the solubility in water is very low, and the water is extremely insoluble; the explosion limit of the mixture with air is 12.5 to 74.2 percent; carbon monoxide is easy to combine with hemoglobin to form carboxyhemoglobin, so that the hemoglobin loses the oxygen carrying capacity and function, and the tissues are suffocated and die when the oxygen carrying capacity and function are serious; carbon monoxide has toxic effects on systemic histiocytes, and especially on the cerebral cortex. Therefore, the direct emission of carbon monoxide is very polluting to the environment. Therefore, due to the requirement of green emission, the denitration treatment and the CO removal treatment of the flue gas are required. The decarbonization and denitration method adopted by the industry at present mainly comprises the step of firstly converting CO in flue gas into CO by a catalytic oxidation method in the prior art2And then carrying out denitration treatment by a selective catalytic reduction method (SCR) and a selective non-catalytic reduction method (SNCR). Wherein, the SCR denitration is to adopt ammonia, urea and the like as reducing agents in the presence of a catalyst and subject the flue gas to the presence of oxygen and under the condition of a certain temperatureReduction of NO in (1) to N2. SNCR is a mature low-cost denitration technology, which takes a hearth or a predecomposition furnace in the cement industry as a reactor, sprays reducing agent containing amino into the hearth, and the reducing agent reacts with NOx in flue gas to generate N2And H2And O. At the same time, processes for NOx removal using CO have also been proposed in the prior art, but because of the higher concentration of O in the flue gas2The reaction of CO to reduce NOx is strongly suppressed, thereby making it difficult to directly apply CO to the denitration process. To solve O2The difficult problem of inhibiting CO from reducing NOx is generally that an adsorption-reduction decoupling denitration process is adopted, namely, the reaction of reducing NOx by CO is artificially divided into two processes of adsorption and reduction, NOx in flue gas is firstly adsorbed on the surface of a catalyst, and then in a separate reduction region, NOx adsorbed on the surface of the catalyst is reduced into N by a reducing agent CO2The NOx adsorption and reduction process is continuously carried out, and the aim of removing NOx in the smoke is fulfilled. However, in the flue gas decarburization and denitration process in the prior art, the utilization efficiency of CO is limited, and meanwhile, the complex adsorption-reduction decoupling denitration process depends on expensive products such as catalysts and adsorbents, so that the production cost is increased, and NH is easy to appear in the process of denitration by an ammonia method3The escape phenomenon causes the problems of blockage of downstream equipment, haze formation in the atmosphere and the like.
The utility model discloses in, through carrying out rational distribution with desulfurization dust removal back flue gas, distribute some flue gas earlier and get into CO catalytic oxidation reaction unit desorption CO, then the remaining part flue gas mixes with the flue gas that has got rid of CO (because a large amount of oxygen have been consumed during CO catalytic oxidation in some flue gas to reduce the oxygen content in the mixed flue gas, further weakened O2Inhibition of reaction of reducing NOx by CO), and finally entering a CO catalytic NOx reduction system for denitration treatment. The scheme of this application has realized: most of CO in flue gas is converted into CO through catalytic oxidation2The reaction heat is removed and supplied to a subsequent denitration system, and simultaneously the oxygen in the flue gas is consumed, thereby further weakening the subsequent O2Suppression of the CO reduction NOx reaction. Meanwhile, the residual CO in the flue gas is used as a reducing agent for denitration reaction to participate in the denitration process, so that the waste is treated by waste, and NH in the denitration process is avoided3The use of vanadium-titanium catalyst and CO denitration adsorbent. Conversion of CO to CO by catalytic oxidation2Meanwhile, a large amount of heat can be released, the heat released in the CO catalytic oxidation process can be fully utilized for subsequent denitration, and the heat supplement of an external heat source to the flue gas is reduced or even avoided.
The utility model discloses in, industrial flue gas, like sintering flue gas etc. particulate matter, sulfur dioxide can get rid of after removing dust, the desulfurization, obtain the raw flue gas that contains CO, NOx. Wherein, a part of raw flue gas containing CO and NOx firstly enters a CO catalytic oxidation reactor, and the CO reacts under the action of a catalyst (such as a noble metal catalyst taking Pt and Pd as main active components) as follows:
2CO+O2→2CO2
after the reaction is finished, NOx-containing smoke is obtained, the reaction process releases heat violently, and the combustion heat of CO is 283 kJ/mol. Meanwhile, the rest of the original flue gas containing CO and NOx is fully mixed with the flue gas containing NOx and enters a carbon monoxide catalytic NOx reduction system, and the CO and the NOx are reacted under the action of a catalyst (such as a noble metal catalyst taking Ir as a main active component):
2CO+2NO→2CO2+N2
through the two-step reaction and a reasonable flue gas flow-dividing treatment mechanism, CO in the original flue gas is fully and efficiently utilized to realize the simultaneous removal of CO and NOx in the original flue gas, the technical effects of treating waste by waste and killing two birds with one stone are achieved, and the obtained clean flue gas enters the atmosphere along with the emission of a chimney.
In the utility model, the arrangement sequence of desulfurization and dust removal can be dust removal → desulfurization, or desulfurization → dust removal, or dust removal → desulfurization → dust removal, etc. The desulfurization process may be a wet process (e.g., limestone/gypsum process), or a semi-dry process (e.g., circulating fluidized bed), or a dry process (e.g., activated carbon process), etc. The dust removal process can be electrostatic dust removal, cloth bag dust removal, electric bag combined dust removal and the like.
The utility model discloses in, for the rational distribution that realizes former flue gas for CO in the partial flue gas can the desorption, and NOx's desorption in all flue gases also can be satisfied to CO in the remaining part flue gas simultaneously, through establishing on the third pipelineThe first flow detection device is arranged for detecting the flow of the flue gas subjected to desulfurization and dust removal in real time as v1 Nm3H is used as the reference value. A second flow detection device is arranged on the fourth pipeline for detecting the flow of the desulfurized and dedusted flue gas distributed to the catalytic oxidation device in real time as v2, Nm3H is used as the reference value. A CO concentration detection device is also arranged in the flue gas flow distribution device for detecting the volume concentration of CO in the flue gas after desulfurization and dust removal to be p1, ppm/Nm3. A NOx concentration detection device is also arranged in the flue gas flow dividing device for detecting the volume concentration r1, ppm/Nm of NOx in the flue gas after desulfurization and dust removal in real time3. The fourth pipeline is also provided with a first valve, and the fifth pipeline is also provided with a second valve. Then, according to the volume concentration balance relationship between the CO and the NOx in the mixed flue gas, the following results are obtained:
v2 × p1 (1-b) + (v1-v2) × p1 ═ a × v1 × r1.
In the formula I, a is a CO surplus coefficient of the content of CO in the catalytic reduction device relative to the content of NOx, and the value is 1-2, preferably 1.1-1.8, and more preferably 1.3-1.5. Generally, in order to ensure that the reaction for catalytic reduction of NOx by CO is carried out more thoroughly, the reducing agent CO should be in a sufficient amount relative to NOx, namely the amount of CO is a times of the theoretical calculation amount, and a is defined as the "CO surplus coefficient".
In the formula I, b is the CO combustion coefficient in the catalytic oxidation device, and is 0.1-1, preferably 0.4-0.95, and more preferably 0.7-0.9.
Further, formula I converts to:
formula II, (v1-a v1 r1/p1)/b.
The flow of the desulfurized and dedusted flue gas which is distributed and conveyed to the catalytic oxidation device through the fourth pipeline is calculated as the value v2, Nm of the formula II by regulating and controlling the first valve3H is used as the reference value. The raw flue gas can be accurately shunted after being calculated by the formula, so that the catalytic oxidation of CO and the reduction reaction of CO catalytic NOx are more thorough.
The utility model discloses in, for the oxygen content in the former flue gas of strict control and make CO catalytic oxidation more thorough, be s1, ppm Nm through be provided with the volume concentration of oxygen among the flue gas behind the oxygen concentration detection device real-time detection desulfurization dust removal in flue gas diverging device, the flue gas diverging device3. Catalytic oxidationThe device is also connected with an oxygen supplementing device through an oxygen pipeline. The oxygen excess coefficient in the catalytic oxidation device is set as c, and the value is 1-2, preferably 1.1-1.8, and more preferably 1.3-1.5. Then:
when s1 is 0.5 × p1 × b × c. The oxygen content is sufficient and the system is not treated.
When s1 < 0.5 × p1 × b × c. And (3) starting an oxygen supplementing device to supplement oxygen-containing gas (such as air and oxygen-enriched gas) into the catalytic oxidation device when the oxygen content is insufficient, wherein the oxygen supplementing quantity is N, ppm:
N＝0.5*v2*p1*b*c-v2*s1.., formula III.
When the oxygen content in the catalytic oxidation device is insufficient, the oxygen supplementing quantity conveyed to the catalytic oxidation device through the oxygen conveying pipeline by the oxygen supplementing device is regulated and controlled to be the calculated value N, ppm of the formula III. The oxygen supplement amount obtained by calculation through the formula can accurately control the oxygen content in the flue gas, and the subsequent CO catalytic NOx reduction reaction is not influenced while the CO catalytic oxidation is met.
The utility model discloses in, be t1, degree C through be provided with the temperature that temperature-detecting device real-time detection desulfurization removed dust back flue gas in flue gas diverging device. The CO catalytic oxidation activation temperature in the catalytic oxidation device is set to t2 and DEG C. Then:
the utility model discloses in, the concurrent heating device is according to the operating mode needs to the selective device of concurrent heating or not concurrent heating of flue gas of flowing through it, and then makes the temperature of the flue gas of concurrent heating device satisfy CO catalytic oxidation temperature requirement that starts to live, and concrete process is as follows:
when t1 ≧ t2, the system does not process.
When t1 is less than t2, the heat supplementing device is started to supplement heat to the desulfurized and dedusted flue gas conveyed to the catalytic oxidation device, wherein the heat supplementing heat is Q1, kJ:
q1 ═ C × v2. (t2-t 1).
In the formula IV, C is the average specific heat capacity of the flue gas after desulfurization and dust removal, and kJ/DEG C.g. The heat quantity for supplementing heat to the desulfurized and dedusted flue gas conveyed to the catalytic oxidation device by starting the heat supplementing device is calculated value Q1, kJ of formula IV.
In the utility model, the water-saving device is provided with a water-saving valve,the seventh pipeline is provided with a heat exchange device. Setting the heat production quantity of CO catalytic oxidation in the catalytic oxidation device to be Q2kJ. The temperature of the mixed flue gas in the flow mixing device is set to be t3 and DEG C. Setting the activation temperature of CO catalytic reduction NOx in the catalytic reduction device to t4At deg.C. Then:
Q2＝b*v2*p1*28/22.4*10-3formula V28 x 283.
t3 ═ t1+ k (Q1+ Q2)/(C × v1).
Substituting formula IV and formula V into formula VI to obtain:
t3＝t1+[k*(t2-t1)*C*v2+k*b*v2*p1*28/22.4*10-3/28*283]v1.
Wherein k is a heat transfer coefficient, and is 0.7-1, preferably 0.8-0.98, and more preferably 0.9-0.95. The heat of combustion of CO was 283 kJ/mol. The relative molecular mass of CO was 28. The volume of any gas of 1mol under standard conditions is 22.4L (here CO gas).
The utility model discloses in, heat transfer device indicates can heat the flue gas of flowing through it, also can carry out the device that cools down to the flue gas of flowing through it, can select heat transfer device to heat or cool down the flue gas of flowing through according to operating condition needs, and concrete process is as follows:
when t3 is t4, the system does not process.
When t3 is less than t4, the heat exchange device is started to heat the mixed flue gas conveyed to the flow mixing device, and the heating heat is Q3, kJ:
q3 ═ C ═ v1.. formula VIII (t4-t 3).
The heat quantity for heating the mixed flue gas conveyed into the flow mixing device by starting the heat exchange device is the calculated value Q3, kJ of the formula VIII.
When t3 is greater than t4, the heat exchange device is started or not started (in practical cases, the temperature at the position is not much higher than the actually required temperature, and the temperature can be optionally not reduced), so that the heat absorption treatment is carried out on the mixed flue gas conveyed into the flow mixing device, and the heat absorption heat is Q4, kJ:
q4 ═ C ═ v1.. formula IX (t3-t 4).
The heat quantity absorbed by the mixed flue gas conveyed into the flow mixing device by starting the heat exchange device is calculated value Q4, kJ of formula IX.
The utility model discloses in, through reasonable setting oxygenating device, concurrent heating device, heat transfer device etc for former flue gas is carrying out CO catalytic oxidation and handles the technological efficiency that combines together with CO catalysis NOx reduction higher, and make full use of the characteristic of former flue gas itself has accomplished the decarbonization denitration treatment to former flue gas, has realized the purpose of treating waste with waste. And meanwhile, a waste heat recovery device is also arranged on the eighth pipeline to recycle the heat in the clean flue gas. And the waste heat in the clean flue gas absorbed by the waste heat recovery device is used for a heat supplementing device or a heat exchange device. When having reduced the thermal emission in the clean flue gas, can also avoid additionally setting up the heat source to the system, reduced the input cost.
The catalytic oxidation device of the utility model is of a box structure, a tower structure or a tubular structure. The catalytic oxidation device comprises a catalyst layer, a flue gas inlet and a flue gas outlet.
Preferably, the height of the catalytic oxidation unit is from 1 to 50m, preferably from 2 to 45m, more preferably from 3 to 40 m.
Preferably, the height of the catalyst layer in the catalytic oxidation unit is 5 to 90%, preferably 8 to 80%, more preferably 10 to 60% of the height of the catalytic oxidation unit.
In the present invention, the height of the desulfurization unit is 2 to 80m, preferably 5 to 60m, and more preferably 8 to 40 m. Compared with the prior art, the utility model discloses a beneficial technological effect as follows:
1. the utility model provides two kinds of technical process of CO desorption and resourceization (CO is as reductant catalytic reduction denitration) to two kinds of technical process have carried out organic combination, have realized the purpose of CO desorption and resourceization high efficiency utilization.
2. The utility model provides a CO catalytic oxidation heat production is used for the system flue gas to heat up, has saved the process that outside fuel heating heaied up this flue gas even, has realized energy saving and consumption reduction.
3. The CO in the utility model is used as a reducing agent to replace the traditional NH3Used as a reducing agent to catalyze and reduce NOx and treat wastes with wastesAvoid NH3And the secondary pollution caused by the use of the traditional vanadium-titanium catalyst.
Drawings
Fig. 1 is a structural diagram of a flue gas treatment system for efficiently utilizing carbon monoxide according to the present invention.
Fig. 2 is a structural diagram of the flue gas treatment system with detection mechanism for efficient utilization of carbon monoxide.
Fig. 3 is a schematic flow chart of the flue gas treatment method of the present invention.
Reference numerals: 1: a desulfurization unit; 2: a dust removal device; 3: a flue gas diversion device; 4: a catalytic oxidation unit; 5: a flue gas flow mixing device; 6: a catalytic reduction device; 7: a heat-supplementing device; 8: an oxygen supplementing device; 9: a heat exchange device; 10: a waste heat recovery device; l1: a first conduit; l2: a second conduit; l3: a third pipeline; l4: a fourth conduit; l5: a fifth pipeline; l6: a sixth pipeline; l7: a seventh pipe; l8: an eighth conduit; v1: a first flow detection device; v2: a second flow detection device; m1: a first valve; m2: a second valve; p: a CO concentration detection device; r: a NOx concentration detection means; s: an oxygen concentration detection device; t: a temperature detection device.
Detailed Description
The technical solution of the present invention is illustrated below, and the claimed invention includes but is not limited to the following embodiments.
The utility model provides a flue gas processing system that carbon monoxide high efficiency was utilized, this system of including desulphurization unit 1, dust collector 2, flue gas diverging device 3, catalytic oxidation device 4, flue gas mixed flow device 5 and catalytic reduction device 6. The raw flue gas duct L1 communicates to the desulfurizer 1. The desulfurization device 1 is communicated to the dust removing device 2 through a second pipeline L2. The dust removing device 2 is communicated to the flue gas flow dividing device 3 through a third pipeline L3. A fourth pipeline L4 is branched from the flue gas branching device 3 and communicated to the catalytic oxidation device 4. A fifth pipeline L5 is further branched from the flue gas flow dividing device 3 and communicated to the flue gas flow mixing device 5. The redox catalytic oxidation device 4 is divided into a sixth pipeline L6 communicated to a fifth pipeline L5. The flue gas flow mixing device 5 is communicated to the catalytic reduction device 6 through a seventh pipeline L7. The catalytic reduction device 6 is communicated to the outside through an eighth pipe L8.
Preferably, the system further comprises a heat supplementing device 7. The heat compensating device 7 is provided on the fourth pipe L4.
Preferably, the system further comprises an oxygen supply device 8. The oxygen supplementing device 8 is connected with the catalytic oxidation device 4 through an oxygen conveying pipeline.
Preferably, the system further comprises a heat exchange device 9. The heat exchange means 9 is disposed on the seventh pipe L7.
Preferably, the system further comprises a waste heat recovery device 10. The waste heat recovery device 10 is disposed on the eighth pipeline L8.
Preferably, the system further comprises a first flow detection device V1. The first flow rate detecting device V1 is provided on the third conduit L3.
Preferably, the system further comprises a second flow detection device V2. The first flow rate detecting device V1 is provided on the third conduit L3.
Preferably, the system further comprises a first valve M1. The first valve M1 is disposed on the fourth pipe L4.
Preferably, the system further comprises a second valve M2. The second valve M2 is provided on the fifth pipe L5.
Preferably, the system further includes a CO concentration detection device P, NOx, a concentration detection device R, an oxygen concentration detection device S, and a temperature detection device T. The CO concentration detection device P, NOx, the concentration detection device R, the oxygen concentration detection device S and the temperature detection device T are all arranged in the smoke diversion device 3.
In the present invention, the catalytic oxidation apparatus 4 has a box structure, a tower structure or a tubular structure. The catalytic oxidation device comprises a catalyst layer, a flue gas inlet and a flue gas outlet.
Preferably, the height of the catalytic oxidation unit 4 is 1 to 50m, preferably 2 to 45m, more preferably 3 to 40 m.
Preferably, the height of the catalyst layer in the catalytic oxidation unit 4 is 5 to 90%, preferably 8 to 80%, more preferably 10 to 60% of the height of the catalytic oxidation unit.
In the present invention, the height of the desulfurization apparatus 1 is 2 to 80m, preferably 5 to 60m, and more preferably 8 to 40 m.
Example 1
As shown in fig. 1, a flue gas treatment system for efficiently utilizing carbon monoxide comprises a desulfurization device 1, a dust removal device 2, a flue gas diversion device 3, a catalytic oxidation device 4, a flue gas flow mixing device 5 and a catalytic reduction device 6. The raw flue gas duct L1 communicates to the desulfurizer 1. The desulfurization device 1 is communicated to the dust removing device 2 through a second pipeline L2. The dust removing device 2 is communicated to the flue gas flow dividing device 3 through a third pipeline L3. A fourth pipeline L4 is branched from the flue gas branching device 3 and communicated to the catalytic oxidation device 4. A fifth pipeline L5 is further branched from the flue gas flow dividing device 3 and communicated to the flue gas flow mixing device 5. The redox catalytic oxidation device 4 is divided into a sixth pipeline L6 communicated to a fifth pipeline L5. The flue gas flow mixing device 5 is communicated to the catalytic reduction device 6 through a seventh pipeline L7. The catalytic reduction device 6 is communicated to the outside through an eighth pipe L8. The height of the catalytic oxidation unit 4 is 20 m.
Example 2
Example 1 is repeated, as shown in fig. 2, except that the system further comprises a heat-replenishing device 7. The heat compensating device 7 is provided on the fourth pipe L4.
Example 3
Example 2 is repeated except that the system further comprises an oxygenating device 8. The oxygen supplementing device 8 is connected with the catalytic oxidation device 4 through an oxygen conveying pipeline.
Example 4
Example 3 was repeated except that the system further included a heat exchange means 9. The heat exchange means 9 is disposed on the seventh pipe L7.
Example 5
Example 4 is repeated except that the system further comprises a waste heat recovery device 10. The waste heat recovery device 10 is disposed on the eighth pipeline L8.
Example 6
Example 5 was repeated except that the system further included a first flow sensing device V1 and a second flow sensing device V2. The first flow rate detecting device V1 is provided on the third conduit L3. The second flow rate detecting device V2 is provided on the fourth pipe L4.
Example 7
Example 6 is repeated except that the system further includes a first valve M1 and a second valve M2. The first valve M1 is disposed on the fourth pipe L4. The second valve M2 is provided on the fifth pipe L5.
Example 8
Example 7 was repeated except that the system further included a CO concentration detecting device P. The CO concentration detection device P is arranged in the flue gas splitting device 3.
Example 9
Example 8 is repeated except that the system further includes NOx concentration detecting means R. The NOx concentration detection device R is arranged in the smoke diversion device 3.
Example 10
Example 9 is repeated except that the system further comprises an oxygen concentration detecting means S. The oxygen concentration detection device S is arranged in the flue gas diversion device 3.
Example 11
Example 10 is repeated except that the system further comprises a temperature sensing means T. The temperature detection device T is arranged in the smoke diversion device 3.
Claims (23)
1. The utility model provides a flue gas processing system that carbon monoxide high efficiency utilized which characterized in that: the system comprises a desulphurization device (1), a dust removal device (2), a flue gas flow dividing device (3), a catalytic oxidation device (4), a flue gas flow mixing device (5) and a catalytic reduction device (6); the original flue gas conveying pipeline (L1) is communicated to the desulphurization device (1); the desulfurization device (1) is communicated to the dust removal device (2) through a second pipeline (L2); the dust removal device (2) is communicated to the flue gas distribution device (3) through a third pipeline (L3); a fourth pipeline (L4) is branched from the flue gas splitting device (3) and communicated to the catalytic oxidation device (4); a fifth pipeline (L5) is also branched from the flue gas flow dividing device (3) and communicated to the flue gas flow mixing device (5); the redox device (4) is divided into a sixth pipeline (L6) communicated to a fifth pipeline (L5); the flue gas flow mixing device (5) is communicated to the catalytic reduction device (6) through a seventh pipeline (L7); the catalytic reduction device (6) is communicated to the outside through an eighth pipeline (L8); wherein: the height of the catalytic oxidation device (4) is 1-50 m.
2. The system of claim 1, wherein: the system also comprises a heat supplementing device (7); the heat supplementing device (7) is arranged on the fourth pipeline (L4).
3. The system according to claim 1 or 2, characterized in that: the system also comprises an oxygen supplementing device (8); the oxygen supplementing device (8) is connected with the catalytic oxidation device (4) through an oxygen conveying pipeline.
4. The system according to claim 1 or 2, characterized in that: the system also comprises a heat exchange device (9); the heat exchange device (9) is arranged on the seventh pipeline (L7).
5. The system of claim 3, wherein: the system also comprises a heat exchange device (9); the heat exchange device (9) is arranged on the seventh pipeline (L7).
6. The system according to any one of claims 1, 2, 5, wherein: the system also comprises a waste heat recovery device (10); the waste heat recovery device (10) is arranged on an eighth pipeline (L8).
7. The system of claim 3, wherein: the system also comprises a waste heat recovery device (10); the waste heat recovery device (10) is arranged on an eighth pipeline (L8).
8. The system of claim 4, wherein: the system also comprises a waste heat recovery device (10); the waste heat recovery device (10) is arranged on an eighth pipeline (L8).
9. The system of any one of claims 1-2, 5, 7-8, wherein: the system also includes a first flow detection device (V1); the first flow rate detecting device (V1) is provided on the third piping (L3).
10. The system of claim 3, wherein: the system also includes a first flow detection device (V1); the first flow rate detecting device (V1) is provided on the third piping (L3).
11. The system of claim 4, wherein: the system also includes a first flow detection device (V1); the first flow rate detecting device (V1) is provided on the third piping (L3).
12. The system of any one of claims 1-2, 5, 7-8, 10-11, wherein: the system also comprises a second flow detection device (V2); the second flow rate detection device (V2) is provided on the fourth conduit (L4).
13. The system of claim 3, wherein: the system also comprises a second flow detection device (V2); the second flow rate detection device (V2) is provided on the fourth conduit (L4).
14. The system of claim 4, wherein: the system also comprises a second flow detection device (V2); the second flow rate detection device (V2) is provided on the fourth conduit (L4).
15. The system of any one of claims 1-2, 5, 7-8, 10-11, 13-14, wherein: the system also includes a first valve (M1); the first valve (M1) is disposed on the fourth pipe (L4).
16. The system of claim 3, wherein: the system also includes a first valve (M1); the first valve (M1) is disposed on the fourth pipe (L4).
17. The system of claim 4, wherein: the system also includes a first valve (M1); the first valve (M1) is disposed on the fourth pipe (L4).
18. The system of any of claims 1-2, 5, 7-8, 10-11, 13-14, 16-17, wherein: the system further comprises a second valve (M2); the second valve (M2) is disposed on the fifth pipe (L5).
19. The system of claim 3, wherein: the system further comprises a second valve (M2); the second valve (M2) is disposed on the fifth pipe (L5).
20. The system of claim 4, wherein: the system further comprises a second valve (M2); the second valve (M2) is disposed on the fifth pipe (L5).
21. The system of any one of claims 1-2, 5, 7-8, 10-11, 13-14, 16-17, 19-20, wherein: the system also comprises a CO concentration detection device (P), a NOx concentration detection device (R), an oxygen concentration detection device (S) and a temperature detection device (T); the CO concentration detection device (P), the NOx concentration detection device (R), the oxygen concentration detection device (S) and the temperature detection device (T) are all arranged in the smoke diversion device (3).
22. The system of claim 3, wherein: the system also comprises a CO concentration detection device (P), a NOx concentration detection device (R), an oxygen concentration detection device (S) and a temperature detection device (T); the CO concentration detection device (P), the NOx concentration detection device (R), the oxygen concentration detection device (S) and the temperature detection device (T) are all arranged in the smoke diversion device (3).
23. The system of claim 4, wherein: the system also comprises a CO concentration detection device (P), a NOx concentration detection device (R), an oxygen concentration detection device (S) and a temperature detection device (T); the CO concentration detection device (P), the NOx concentration detection device (R), the oxygen concentration detection device (S) and the temperature detection device (T) are all arranged in the smoke diversion device (3).
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| CN113251793A (en) * | 2021-05-17 | 2021-08-13 | 中冶长天国际工程有限责任公司 | Oxygen-enriched low-CO sintering method, oxygen-enriched low-CO sintering machine and control method thereof |
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| CN113251793A (en) * | 2021-05-17 | 2021-08-13 | 中冶长天国际工程有限责任公司 | Oxygen-enriched low-CO sintering method, oxygen-enriched low-CO sintering machine and control method thereof |
| CN113251793B (en) * | 2021-05-17 | 2022-06-03 | 中冶长天国际工程有限责任公司 | Oxygen-enriched low-CO sintering method, oxygen-enriched low-CO sintering machine and control method thereof |
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