CN112675702A - SCR denitration method and device - Google Patents
SCR denitration method and device Download PDFInfo
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- CN112675702A CN112675702A CN202011637455.6A CN202011637455A CN112675702A CN 112675702 A CN112675702 A CN 112675702A CN 202011637455 A CN202011637455 A CN 202011637455A CN 112675702 A CN112675702 A CN 112675702A
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Abstract
The invention relates to an SCR denitration method and device. The method comprises the following steps: the flue gas passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in one direction to be denitrated; the denitrated flue gas passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in sequence in a one-way mode to be denitrated; the activity temperature of the first catalyst is 120-350 ℃; the activity temperature of the second catalyst is 200-450 ℃. The technical problem to be solved is how to effectively denitrate the flue gas with the temperature fluctuating in a wider range, SO that the problems of nitrogen oxide emission exceeding standard, ammonia escape increasing and the like are avoided, and the problem that the SO is caused by reducing the activity temperature of the catalyst is avoided2/SO3The conversion rate is improved to cause the problem of sulfur poisoning, and the effective denitration during the full-load operation of the system can be met, so that the device is suitable for the potThe flue gas temperature change caused by frequent fluctuation of the furnace load realizes stable ultralow emission of nitrogen oxide and ammonia, thereby being more practical.
Description
Technical Field
The invention relates to the technical field of tail end treatment of nitrogen oxides in industrial flue gas, in particular to an SCR denitration method and device.
Background
The SCR denitration technology is a flue gas nitrogen oxide emission reduction technology commonly adopted in the industries of thermal power, building materials, coking and the like in China. In recent years, with the development of the blue sky defense war and the like, the national environmental protection department and each province and city region make implementation schemes and detailed rules, and the industry is required to adopt measures such as load reduction and the like to reduce the total pollutant emission, so that the smoke temperature frequently fluctuates in a wider interval. For example, the load of the power plant is usually adjusted at 35-100%, and when the power plant boiler runs at full load, the flue gas temperature is about 370 ℃; when the load is reduced to 50%, the temperature is about 310 ℃; when the load is reduced to 35%, the temperature is only about 250 ℃.
The vanadium content of conventional vanadium-titanium based catalysts is generally<1 percent, the active temperature zone is 350-450 ℃, and the method is suitable for the smoke temperature during full-load operation; when the system operates at low load, the problems of nitrogen oxide emission exceeding standard, increased ammonia escape and the like are caused, and meanwhile, the corrosion of a tail end pipeline and equipment is easily caused. While increasing the vanadium content of the catalyst may lower the activation temperature, but SO2/SO3The conversion rate is improved, sulfur poisoning is easy to occur, and the method is not suitable for the working condition during full-load operation.
In order to solve the above technical problems, researchers in the field propose the following two routes:
one is to develop a denitration catalyst with a wide temperature window, but the research is still in the research and development stage of a laboratory at present and cannot be popularized and used industrially.
Secondly, a coal-fired boiler and an SCR system are reformed to improve the smoke temperature under the low-load operation condition, but the following problems exist: 1) the scheme only discloses that the flue gas temperature of the coal-fired boiler can reach 320 ℃ under the working condition of 50% load, but the flue gas temperature under the working condition of lower load is not simulated, so that the technical problem cannot be solved; 2) the coal-fired boiler is additionally provided with the economizer flue gas bypass and the economizer pipe group is rearranged, and the economic efficiency of the unit is easily reduced due to the large difficulty in equipment transformation; meanwhile, the exhausted flue gas is reheated to cause energy waste.
Disclosure of Invention
The invention mainly aims to provide an SCR denitration method and device, and aims to solve the technical problems of effectively denitrating flue gas with temperature fluctuating in a wider temperature range, avoiding the problems of nitrogen oxide emission exceeding standard, ammonia escape increasing and the like caused by low-load operation of a system and avoiding SO caused by reduction of the activity temperature of a catalyst when the system is in low-load operation2/SO3The conversion rate is improved and the problem of sulfur poisoning is caused, and effective denitration during full-load operation of the system can be simultaneously met, the flue gas temperature change caused by frequent fluctuation of the load of the boiler (kiln) is adaptable, and stable ultralow emission of nitrogen oxide and ammonia is realized, so that the method is more practical.
The purpose of the invention and the technical problem to be solved are realized by adopting the following technical scheme. The invention provides an SCR denitration method, which comprises the following steps:
1) the flue gas passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in one direction to be denitrated; the temperature of the flue gas is 150-450 ℃;
2) the flue gas subjected to denitration in the step 1) is subjected to denitration by sequentially passing through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in a one-way mode;
wherein the activity temperature of the first catalyst is 120-350 ℃; the activity temperature of the second catalyst is 200-450 ℃.
The object of the present invention and the technical problems solved thereby can be further achieved by the following technical measures.
Preferably, the SCR denitration method includes the steps of:
1) the flue gas sequentially passes through the ceramic heat accumulator, the first catalyst, the reducing agent, the second catalyst, the first catalyst and the ceramic heat accumulator from bottom to top; the reducing agent is injected from bottom to top;
2) the flue gas after denitration in the step 1) sequentially passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator from top to bottom.
Preferably, the SCR denitration method further includes injecting the flue gas with a reducing agent before step 1).
Preferably, the SCR denitration method further includes a step of heating flue gas between step 1) and step 2).
Preferably, in the SCR denitration method, the reducing agent is ammonia or urea.
Preferably, the SCR denitration method further includes detecting the content of nitrogen oxides in the flue gas after step 2);
if the content of the nitrogen oxides is less than or equal to the set standard, the flue gas is discharged;
if the content of the nitrogen oxides is larger than the set standard, denitrating the flue gas according to the following steps A and B or steps A 'and B':
A. the flue gas passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in one direction to be denitrated;
B. b, the flue gas subjected to denitration in the step A is subjected to denitration by sequentially passing through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in a one-way mode;
a', the flue gas sequentially passes through the ceramic heat accumulator, the first catalyst, the reducing agent, the second catalyst, the first catalyst and the ceramic heat accumulator from bottom to top; the reducing agent is injected from bottom to top;
b ', the flue gas subjected to denitration in the step A' sequentially passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator from top to bottom.
Preferably, in the SCR denitration method, the first catalyst is selected from a vanadium-based catalyst with a vanadium content of 2% or more and/or a manganese-based catalyst; the second catalyst is selected from a vanadium-based catalyst and/or a vanadium-titanium catalyst with the vanadium content less than or equal to 3.5 percent.
The object of the present invention and the technical problem to be solved are also achieved by the following technical means. According to the invention, the SCR denitration device comprises:
the reactor comprises a plurality of reaction units which are arranged in parallel; each reaction unit is sequentially provided with a ceramic heat storage layer, a first catalyst bed layer, a second catalyst bed layer, a first catalyst bed layer and a ceramic heat storage layer from bottom to top; the tops of the reaction units are communicated with each other; the bottom of the reaction unit is provided with a flue gas input pipe and a flue gas output pipe; the flue gas input pipe and the flue gas output pipe are both provided with switches;
the flue gas input main pipe is respectively connected with the flue gas input pipes;
and the smoke output main pipe is respectively connected with the smoke output pipes.
The object of the present invention and the technical problems solved thereby can be further achieved by the following technical measures.
Preferably, in the SCR denitration device, the reaction unit is provided with a ceramic heat storage layer, a first catalyst bed layer, a reducing agent spray gun, a second catalyst bed layer, a first catalyst bed layer and a ceramic heat storage layer from bottom to top in sequence;
the SCR denitration device further includes:
a reductant storage tank;
one end of the reducing agent injection system is connected with the reducing agent storage tank, and the other end of the reducing agent injection system is connected with the reducing agent spray gun; a switch is arranged between the reducing agent injection system and the reducing agent spray gun; when the switch is turned on, the reducing agent spray gun can spray the reducing agent from bottom to top.
Preferably, the SCR denitration device further includes a reducing agent injection system; the reducing agent injection system is also connected with the flue gas input main pipe; a switch is arranged between the reducing agent injection system and the flue gas input main pipe; and when the switch is turned on, the reducing agent injection system can inject the reducing agent into the flue gas input manifold.
Preferably, in the SCR denitration device, the ceramic heat storage layer, the first catalyst bed layer, the reducing agent spray gun, the second catalyst bed layer, the first catalyst bed layer, and the ceramic heat storage layer are detachably connected; and the relative distances among the ceramic heat storage layer, the first catalyst bed layer, the reducing agent spray gun, the second catalyst bed layer, the first catalyst bed layer and the ceramic heat storage layer can be adjusted.
Preferably, the SCR denitration device further includes a combustor; the burners are disposed in a region where the tops of the reaction units communicate with each other.
Preferably, in the reaction unit, when the switch of the flue gas input pipe is turned on and the switch of the flue gas output pipe is turned off, the reaction unit can move the flue gas from bottom to top, and the reaction unit at this time is defined as a class I reaction unit; when the switch of the flue gas input pipe is closed and the switch of the flue gas output pipe is opened, the reaction unit can enable the flue gas to move from top to bottom, and the reaction unit at the moment is defined as a II-type reaction unit;
and when the SCR denitration device works, the switch of the reducing agent spray gun in the I-type reaction unit is turned on, and the switch of the reducing agent spray gun in the II-type reaction unit is turned off.
Preferably, in the SCR denitration device, the flow direction of the flue gas in the reaction unit can be changed by changing the on-off state of the flue gas input pipeline and the on-off state of the flue gas output pipeline of the reaction unit.
Preferably, in the SCR denitration device, the number of the reaction units is 2 to 10.
By the technical scheme, the SCR denitration method and the device provided by the invention at least have the following advantages:
1. the SCR denitration method and the device provided by the invention have the advantages that through the combined use of catalysts in various systems and wide temperature range intervals, the addition of ceramic heat storage layers at the upper end and the lower end of the reaction unit, the optimized arrangement of a reducing agent injection system, flue gas circulation reversing, flue gas reheating by installing a burner and other technical measures, the SCR denitration device can effectively denitrate low-temperature flue gas of a boiler in low-load operation and high-temperature flue gas of the boiler in full-load operation, the technical problem that the denitration is difficult due to the change of the flue gas temperature of the boiler in the wide temperature range under different load operation conditions is perfectly solved, and the flue gas denitration with the change of the boiler load can be realized by using one set of SCR denitration device;
2. the SCR denitration method and the device provided by the invention can effectively denitrate in a wide temperature range of 150-450 ℃, can adapt to the flue gas temperature change caused by frequent fluctuation of the load of a boiler (kiln) and realize stable ultralow emission of nitrogen oxides and ammonia.
The foregoing description is only an overview of the technical solutions of the present invention, and in order to make the technical solutions of the present invention more clearly understood and to implement them in accordance with the contents of the description, the following detailed description is given with reference to the preferred embodiments of the present invention and the accompanying drawings.
Drawings
FIG. 1 is a schematic diagram of a technological principle of a wide temperature zone SCR denitration technology provided by an embodiment of the invention;
FIG. 2 is a schematic diagram of a wide temperature zone SCR denitration technology and device provided by an embodiment of the invention;
FIG. 3 is a denitration activity curve according to an example of the present invention.
Detailed Description
To further illustrate the technical means and effects of the present invention adopted to achieve the predetermined objects, the following detailed description will be made on the specific implementation, structure, features and effects of an SCR denitration method and apparatus according to the present invention with reference to the accompanying drawings and preferred embodiments.
The invention provides an SCR denitration method, which comprises the following steps as shown in the attached figure 1:
1) the flue gas passes through the ceramic heat accumulator 1, the first catalyst 2, the second catalyst 3, the first catalyst 2 and the ceramic heat accumulator 1 in sequence in a one-way mode to be denitrated; the temperature of the flue gas is 150-450 ℃;
2) the flue gas subjected to denitration in the step 1) is subjected to denitration by sequentially passing through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in a one-way mode;
wherein the activity temperature of the first catalyst is 120-350 ℃; the activity temperature of the second catalyst is 200-450 ℃.
In the flow direction of the flue gas in the technical scheme, the unidirectional flow in the step 1) can be from bottom to top, or from left to right, and the flow direction is not limited; the direction of the unidirectional flow in the step 2) can be the same as or opposite to the flow direction of the smoke in the step 1); how the flue gas flow direction is set can be set according to the actual situation of a production field.
The core of the technical scheme is that the flue gas temperature is stable and the flue gas is rectified through catalyst type selection, catalyst arrangement sequence and a ceramic heat accumulator, so that the flue gas denitration under the condition that the flue gas temperature frequently fluctuates in a large range caused by the change of the production load of the kiln can be realized by only one set of device and one method, and the flue gas of the kiln under various working conditions can be effectively denitrated.
According to the technical scheme, the ceramic heat accumulators are arranged at the two ends of the catalyst to adjust the flue gas temperature during denitration so as to stabilize the catalyst, so that the denitration difficulty caused by the fluctuation of the flue gas temperature is reduced. For example, assuming a kiln flue gas temperature of 200-400 ℃, if the kiln is operated at a full load, the flue gas temperature is 400 ℃, which may be 30% (the full load operation time is the proportion of the total operation time); the operating flue gas temperature under 80% load condition is 300 ℃, and the proportion of the operating flue gas temperature in the case can be 60%; the operating flue gas temperature at 50% load is 200 ℃, which may be 10%. According to the technical scheme, ceramic heat accumulators are arranged at two ends of the catalyst; the ceramic heat accumulator mainly has the functions of better stabilizing the temperature of the flue gas and improving the uniformity of a flue gas flow field. Specifically, when the temperature of the flue gas is higher, the ceramic heat accumulator can absorb the heat in the flue gas to store heat for later use, and simultaneously can reduce the temperature of the flue gas at the moment; when the temperature of the flue gas is lower, the ceramic heat accumulator can release heat to heat the flue gas so as to improve the temperature of the flue gas at the moment. Through the arrangement of the ceramic heat accumulator, the temperature of the flue gas discharged by the kiln is effectively adjusted, and the range of the temperature of the flue gas is correspondingly reduced, so that the difficulty of wide-temperature denitration is reduced, and the efficiency of flue gas denitration is improved.
Furthermore, ceramic heat accumulators are arranged at two ends of a catalyst combination of the first catalyst, the second catalyst and the first catalyst, and are used for collecting and utilizing waste heat of the flue gas and effectively transferring the heat to the catalysts in addition to stabilizing the flue gas temperature and reducing the width between the upper limit and the lower limit of the flue gas temperature, so that the catalysts can work at a certain temperature, nitrate in the flue gas can be effectively eliminated, and energy can be saved; on the other hand, the flue gas enters from one end of one unit and flows out from one end of a second unit, namely the flue gas flows in the whole reactor; the ceramic heat accumulator is of a honeycomb structure, the uniformity of a flue gas flow field can be improved, namely the honeycomb ceramic heat accumulator is equivalent to a flue gas rectifier and can play a role in flue gas rectification.
Furthermore, the flue gas denitration is realized through the model selection of the first catalyst and the second catalyst and the strict arrangement sequence of the first catalyst and the second catalyst, so that the flue gas denitration has higher efficiency. When the first catalyst and the second catalyst are selected, the first catalyst and the second catalyst should have reactivity to the flue gas in all temperature sections as far as possible. The first catalyst is also called a medium/low temperature catalyst; the second catalyst is also known as a medium/high temperature catalyst. The first catalyst and the second catalyst both comprise medium-temperature catalysts, the working temperatures of the medium-temperature catalysts have larger intersection, and proper catalyst combinations can be selected according to different components of flue gas in actual production. Under different denitration conditions, the same catalyst is sometimes used as the first catalyst and sometimes used as the second catalyst. Under the same denitration condition, the working temperature of the first catalyst is lower than that of the second catalyst.
Preferably, the activity temperature of the first catalyst is 200-350 ℃; the activity temperature of the second catalyst is 300-400 ℃.
Further, the arrangement order of the first catalyst, the second catalyst and the first catalyst in the above technical solution is strictly defined, and the reason for this arrangement is that: during the SCR reaction several reactions may occur:
2NO+O2→2NO2 (1)
4NH3+4NO+O2→4N2+6H2O (2)
2NH3+NO+NO2→2N2+3H2O (3)
4NH3+2NO2+O2→3N2+6H2O (4)
the most commonly used medium-high temperature catalyst, such as a vanadium-titanium SCR catalyst, has an active temperature range of 300-450 ℃, the reaction occurring in the flue gas denitration process at the temperature range is generally a reaction formula (2) and is called as standard SCR (standard SCR), and the medium-low temperature SCR catalyst has low activity for the flue gas at the temperature range, and the reason of the low activity is that: one is that V is increased in the medium-low temperature catalyst2O5The content of (A); secondly, transition metal oxides such as Mn, Ce and the like are adopted in the medium-low temperature catalyst, and the catalyst generally has better oxidability and is easy to oxidize NO into NO2. Research shows that NO2Has stronger reaction activity and can be converted into HNO on the surface of the catalyst2Then with NH3The catalytic reaction takes place fast, the denitration reaction rate can be greatly improved, and the reaction efficiency is improved. Thus, NO in general2The participating SCR reaction is called fast SCR (fast SCR).
In the operation process of the industrial kiln, only two working conditions of normal kiln operation and low kiln load operation exist, wherein the low load is referred to as low loadThe operation refers to manual regulation and control according to environmental protection requirements, production requirements and the like, so that the temperature of the flue gas is reduced, and the total amount of the flue gas is reduced. According to the technical scheme, when the catalyst is selected, the flue gas temperatures under two operating conditions are fully considered, and the active temperature intervals of the selected medium-high temperature catalyst and the medium-low temperature catalyst cover the flue gas temperatures under a normal operating state as much as possible, so that all the catalysts can play a denitration role under the normal operating state of the kiln, and the investment cost is reduced. When the production system needs to be adjusted to a low-load working condition, the temperature of the flue gas is reduced, the flue gas firstly passes through the medium-low temperature SCR catalyst, and the nitrogen oxide in the flue gas can undergo an oxidation reaction to oxidize NO into NO2Therefore, the rapid SCR reaction of the flue gas is facilitated, and the subsequent catalyst, namely the second catalyst and the first catalyst, can be subjected to the rapid SCR reaction, so that the efficiency of the denitration reaction and the denitration rate are improved; furthermore, a medium-low temperature catalyst is arranged behind the medium-high temperature catalyst, so that the oxidation reaction of nitrogen oxides in the flue gas is realized to oxidize NO into NO2The reaction is continuously generated, so that the rapid SCR reaction is favorably generated to improve the reaction efficiency and the denitration rate; on the other hand, the high-temperature catalyst can play a role to the maximum extent by adopting a medium-low temperature-medium-high temperature-medium-low temperature catalyst arrangement mode. Furthermore, the flue gas reversing flow is preferably set in the technical scheme of the invention, so that the arrangement modes of medium-low temperature-medium-high temperature-medium-low temperature catalysts are bilaterally symmetrical, and the flue gas denitration reaction after the flue gas reversing is not influenced.
In a specific embodiment of the above technical solution, the flue gas rises from the left unit from bottom to top along the route shown by the thick frame arrow in fig. 1, enters the adjacent unit from the communication position of the top after reaching the top, and falls from the right unit from top to bottom. When the denitration of the flue gas reaches the set emission level, the flue gas can flow out; when the denitration of the flue gas does not reach the set emission level, the flue gas continues to be circularly denitrated along the route shown by the dotted line in the attached figure 1. When the flue gas reaches the bottom of the left unit along the route shown by the dotted line, the flue gas can flow out if the denitration of the flue gas reaches the set emission level; and when the denitration of the flue gas does not reach the set emission level, repeating the process route. The schematic diagram of the attached figure 1 only shows the process method and the flue gas route and flow direction, and the flue gas reversing operation can realize the flue gas reversing at any time by switching the flue gas inlet pipe and the flue gas outlet pipe.
In practice, the different reaction units may be connected in series. In the series connected zones, the flue gas may be reheated to maintain its temperature for higher denitration activity.
When the denitration of the flue gas does not reach the emission level, the flue gas can be returned to the flue gas input pipe through a pipeline to be combined with the new flue gas to be denitrated for post-treatment; or the flue gas can be introduced into the next denitration unit connected with the denitration unit in series through a pipeline to continue denitration.
In the two adjacent smoke circulations, the smoke directions can be the same; at the moment, the flow direction of the flue gas in the flue gas inlet pipe and the flue gas outlet pipe can be adjusted at any time through switching of the flue gas inlet pipe and the flue gas outlet pipe; however, this design may make the denitration apparatus long and inconvenient for field layout.
In the two adjacent flue gas circulations, the flue gas directions can be opposite, namely the flue gas circulates repeatedly in an up-down-up-down direction; the flow directions of the two adjacent smoke flows are opposite, and the smoke flow field distribution is mainly considered. In actual operation, mixing of the flue gases from the headspace will occur and eventually flow out of the reactor from adjacent units.
According to the technical scheme, multiple technical means are combined, the temperature interval of the flue gas is reduced through the adjustment of the ceramic heat accumulator, the reaction difficulty is reduced, and meanwhile the ceramic heat accumulator rectifies the flue gas to optimize the flow field of the flue gas; by combining catalysts in different temperature intervals and optimizing the process route of SCR (selective catalytic reduction), all the catalysts participate in denitration reaction for high-temperature flue gas, and NO is oxidized into NO for low-temperature flue gas2So that the catalyst is subjected to rapid SCR reaction, the reaction rate of other catalysts is accelerated, the denitration rate is improved, the temperature interval of the denitration reaction is widened, and the method is usedCan meet the denitration under the scene of flue gas temperature change caused by frequent fluctuation of the load of the coal-fired boiler (kiln).
Preferably, it comprises the following steps: 1) the flue gas sequentially passes through the ceramic heat accumulator, the first catalyst, the reducing agent, the second catalyst, the first catalyst and the ceramic heat accumulator from bottom to top; the reducing agent is injected from bottom to top; 2) the flue gas after denitration in the step 1) sequentially passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator from top to bottom.
The flow direction of the flue gas in the step 1) is opposite to that of the flue gas in the step 2). In the step 1), namely in the process that the flue gas flows from bottom to top, a reducing agent injection process is arranged between the first catalyst and the second catalyst, and the reducing agent is injected from bottom to top, namely the injection direction of the reducing agent is the same as the flow direction of the flue gas; the reducing agent and the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator are subjected to denitration, so that the denitration efficiency is further improved; in the step 2), the injection of the reducing agent is not started, because the ammonia remained in the process that the flue gas flows from bottom to top can be used as the reducing agent to react in the process that the flue gas flows from bottom to top, and the technical means can reduce the problem of ammonia escape in the denitration process.
Preferably, step 1) is preceded by injecting the flue gas with a reducing agent. Under different working conditions of the flue gas, the reducing agent can be sprayed at the front end of the flue gas entering the reactor, and also can be sprayed in the reaction process, so that the reducing agent can be selected and used under specific working conditions in actual production.
The specific choice of the reducing agent can be specifically determined according to the composition of the flue gas and the actual situation, and ammonia or urea is preferred.
Preferably, a step of heating flue gas is further included between the step 1) and the step 2).
According to the technical scheme, the burners are arranged at two ends of the communicated area at the upper end of the reaction unit, and when the temperature of the flue gas is lower than the active temperature range of the catalyst, the flue gas can be reheated by the burners for a proper time so as to improve the temperature of the flue gas to the active temperature range of the catalyst system; furthermore, part of heat of the combustor can also be stored by a ceramic heat accumulator at the upper end of the reactor to stabilize the temperature of the flue gas. The flue gas is heated additionally to ensure that the temperature of the flue gas is in a proper temperature range, so that the flue gas denitration effect is ensured. Both ends of the smoke heating area are ceramic heat accumulators; when heating the flue gas through the combustor, the flue gas temperature is higher, and the ceramic heat accumulator can store heat this moment and adjust the flue gas temperature in order to be equipped with the later stage, can reduce among the denitration process and open the heater for the frequency of flue gas concurrent heating, cost-economy.
Preferably, detecting the content of nitrogen oxide in the flue gas is also included after the step 2); if the content of the nitrogen oxides is less than or equal to the set standard, the flue gas is discharged; if the content of the nitrogen oxides is larger than the set standard, denitrating the flue gas according to the following steps A and B or steps A 'and B':
A. the flue gas passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in one direction to be denitrated;
B. b, the flue gas subjected to denitration in the step A is subjected to denitration by sequentially passing through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in a one-way mode;
a', the flue gas sequentially passes through the ceramic heat accumulator, the first catalyst, the reducing agent, the second catalyst, the first catalyst and the ceramic heat accumulator from bottom to top; the reducing agent is injected from bottom to top;
b ', the flue gas subjected to denitration in the step A' sequentially passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator from top to bottom.
The emission standards of nitrogen oxides are as follows: the current national standard limit is 400mg/m3The limit value of the control standard of the key area is 320mg/m3(ii) a In the local standard or environmental protection scheme released by many provinces and cities in recent two years, the emission limit is required to be 100mg/m3The following. In actual operation, the method can be selected and applied according to local actual conditions.
The specific selection of the first catalyst and the second catalyst can be specifically determined according to the composition of the flue gas and the actual situation. Preferably, the first catalyst is selected from a vanadium-based catalyst and/or a manganese-based catalyst with the vanadium content of more than or equal to 2 percent; the second catalyst is selected from a vanadium-based catalyst and/or a vanadium-titanium catalyst with the vanadium content less than or equal to 3.5 percent.
The invention also provides an SCR denitration device, as shown in fig. 2, which includes:
the reactor comprises a plurality of reaction units which are arranged in parallel; each reaction unit is sequentially provided with a ceramic heat storage layer 1, a first catalyst bed layer 2, a second catalyst bed layer 3, a first catalyst bed layer 2 and a ceramic heat storage layer 1 from bottom to top; the tops of the reaction units are communicated with each other; the bottom of the reaction unit is provided with a flue gas input pipe and a flue gas output pipe; the flue gas input pipe and the flue gas output pipe are both provided with a switch 8;
the flue gas input main pipe 6 is respectively connected with the flue gas input pipes;
and the smoke output main pipe 7 is respectively connected with the smoke output pipes.
The number of the reaction units is more than or equal to 2. The flue gas to be denitrated enters a reaction unit from a flue gas input pipeline at the bottom of the reaction unit, sequentially passes through a ceramic heat storage layer 1, a first catalyst bed layer (middle/low temperature catalyst bed layer) 2, a second catalyst bed layer (middle/high temperature catalyst bed layer) 3, a first catalyst bed layer (middle/low temperature catalyst bed layer) 3 and a ceramic heat storage layer 4, and then enters a space at the top of a reactor, namely a communication part of the reaction unit; then the flue gas enters a second reaction unit, sequentially passes through a ceramic heat storage layer 1, a first catalyst bed layer (middle/low temperature catalyst bed layer) 2, a second catalyst bed layer (middle/high temperature catalyst bed layer) 3, a first catalyst bed layer (middle/low temperature catalyst bed layer) 2 and a ceramic heat storage layer 1, and then the denitrated flue gas flows out from a flue gas output pipe at the bottom of the reaction unit.
Preferably, the SCR denitration device may further inject a reducing agent; the reducing agent may optionally be injected in the front end of and/or within the reactor.
Preferably, the reaction unit is sequentially provided with a ceramic heat storage layer 1, a first catalyst bed layer 2, a reducing agent spray gun 4, a second catalyst bed layer 3, a first catalyst bed layer 1 and a ceramic heat storage layer 1 from bottom to top; the SCR denitration device further includes: a reducing agent storage tank 10; the reducing agent injection system 9 is connected with the reducing agent storage tank 10 at one end and connected with the reducing agent spray gun 4 at the other end; a switch is arranged between the reducing agent injection system 9 and the reducing agent spray gun 4; when the switch is turned on, the reducing agent spray gun 4 can spray the reducing agent from bottom to top.
Preferably, it also comprises a reducing agent injection system 9; the reducing agent injection system 9 is also connected with the flue gas input main pipe 6; a switch is arranged between the reducing agent injection system 9 and the flue gas input main pipe 6; when the switch is turned on, the reducing agent injection system 9 can inject the reducing agent into the flue gas input manifold 6.
During flue gas denitration, the injection amount of the reducing agent can be adjusted according to the working condition and the running condition of the kiln flue gas and the reaction characteristics. According to actual conditions, only the reducing agent spray gun can be opened to spray the reducing agent; or only the switch of the flue gas input main pipe is opened to find the reducing agent to be injected into the flue gas input main pipe; or the switch of the reducing agent spray gun and the switch of the flue gas input main pipe can be simultaneously opened to simultaneously spray the reducing agent.
Preferably, the ceramic heat storage layer 2, the first catalyst bed layer 2, the reducing agent spray gun 4, the second catalyst bed layer 3, the first catalyst bed layer 2 and the ceramic heat storage layer 1 are detachably connected; the reaction unit comprises a wall body; the ceramic heat storage layer, the first catalyst bed layer, the reducing agent spray gun, the second catalyst bed layer, the first catalyst bed layer and the ceramic heat storage layer are detachably arranged on the wall body; and the relative distances among the ceramic heat storage layer 2, the first catalyst bed layer 2, the reducing agent spray gun 4, the second catalyst bed layer 3, the first catalyst bed layer 2 and the ceramic heat storage layer 1 can be adjusted.
Preferably, a combustor 5 is arranged in a communication area at the upper end of the reaction unit, and when the temperature of the flue gas is lower than a design value or the system is started, the flue gas is reheated to enable the temperature to be stabilized in a catalyst reaction activity window.
During flue gas denitration, the height of each catalyst layer can be designed according to the working condition and the running condition of the flue gas of the furnace and the selected catalyst system. Furthermore, in the actual production, catalyst material systems, catalyst dosage, catalyst hole number, catalyst length and catalyst arrangement modes of different beds can be selected according to the temperature range and fluctuation frequency of the flue gas of the boiler (kiln).
Preferably, in the reaction unit, when the switch of the flue gas input pipe is opened and the switch of the flue gas output pipe is closed, the reaction unit can enable the flue gas to move from bottom to top, and the reaction unit at this time is defined as a type I reaction unit; when the switch of the flue gas input pipe is closed and the switch of the flue gas output pipe is opened, the reaction unit can enable the flue gas to move from top to bottom, and the reaction unit at the moment is defined as a II-type reaction unit; and when the SCR denitration device works, the switch of the reducing agent spray gun in the I-type reaction unit is turned on, and the switch of the reducing agent spray gun in the II-type reaction unit is turned off.
In the SCR denitration device, a reducing agent spray gun in a reaction unit is arranged between two catalyst bed layers at the lower section of the reaction unit, and sprays a reducing agent from bottom to top, and the reducing agent spray gun only sprays in the reaction unit with the same flow direction as flue gas, namely the reducing agent spray gun only can occur in a type I reaction unit; after the flue gas enters the second-class reaction unit from the first-class reaction unit from the top of the reactor, the residual ammonia in the first-class reaction unit can be used as a reducing agent in the second-class reaction unit, so that ammonia escape can be reduced.
Specifically, the parameters of the ammonia injection system can be optimized according to the working condition of the flue gas of the boiler (kiln).
Preferably, the flue gas flow direction in the reaction unit can be changed by changing the on-off state of the flue gas input pipeline and the on-off state of the flue gas output pipeline of the reaction unit.
Specifically, a specific reaction unit can be used as both a class I reaction unit and a class II reaction unit, and the change of the flow direction of the flue gas in the reaction unit, that is, the change of the type of the reaction unit, can be realized only by adjusting the switching state of the flue gas pipeline at the bottom of the reaction unit. Through the change of the type of the reaction unit, namely the change of the flow direction of the flue gas in the reaction unit, the deposition of dust and the escape of ammonia in the reaction unit can be reduced.
Specifically, the flue gas reversing logic can be determined according to the working condition of the flue gas of the boiler (kiln).
Preferably, the number of the reaction units is 2-10. In actual production, flue gas treatment can be carried out by adopting a mode of connecting a plurality of reaction units in parallel according to the working condition of the flue gas of the boiler (kiln) so as to adapt to different working conditions in actual production.
According to the technical scheme, by jointly using catalysts in various systems and wide temperature zone intervals, and by adopting technical means of increasing ceramic heat storage layers at the upper end and the lower end of the reaction unit and optimizing the arrangement of a reducing agent injection system and flue gas circulation reversing, the SCR denitration device disclosed by the invention can effectively denitrate low-temperature flue gas during low-load operation of the boiler and high-temperature flue gas during full-load operation of the boiler, the technical problem that the flue gas temperature of the boiler changes in the wide temperature intervals under different load operation conditions and is difficult to denitrate is perfectly solved, and the flue gas denitration device can be suitable for denitration of flue gas with changed boiler load.
The denitration method and the denitration device in the technical scheme can keep higher denitration activity within the temperature range of 150-450 ℃.
The technical solution of the present invention is further described in detail by the following more specific examples.
Example 1
260000Nm of flue gas volume of an industrial kiln3The temperature of the flue gas is 180-430 ℃, and NO in the flue gasxThe concentration is 500mg/m3，SO2The concentration is 300mg/m3Dust concentration 30g/m3。
(1) Determining the type of the catalyst according to the temperature range of the flue gas:
the first catalyst (medium-low temperature SCR catalyst) adopts a high vanadium catalyst (vanadium content is 4%), and the active temperature range is 170-350 ℃; the second catalyst (medium-high temperature catalyst) adopts a low-vanadium catalyst (vanadium content is 1%), and the active temperature is 280-450 ℃;
(2) determining reactor parameters according to the amount of flue gas:
the reactor was arranged with 4 reaction units (as shown in fig. 2), each layer being arranged with 6 catalyst modules;
(3) determining the dosage of each catalyst according to the components of the flue gas:
the medium-low temperature catalyst is 150X 900mm, 13 holes, and the dosage is 17.5m3A unit;
the medium-high temperature catalyst has 150X 1000mm and 15 holes, and the dosage is 9.7m3A unit;
the total catalyst consumption is 108.8m3。
The denitration device and the denitration method provided by the embodiment of the invention are used for denitration of the flue gas, the denitration activity curve of the flue gas in a wide temperature range of 150-450 ℃ is shown in the attached drawing 3, as can be seen from the denitration curve shown in the attached drawing 3, the denitration efficiency of the flue gas at 180 ℃ can reach 85%, the denitration efficiency gradually rises to the highest point along with the increase of the temperature of the flue gas, the denitration efficiency can reach 96%, and the denitration efficiency is slightly reduced but can still reach more than 80% after the temperature of the flue gas exceeds 350 ℃, namely the denitration method and the denitration device provided by the embodiment of the invention can realize effective denitration in the wide temperature range of 180-450 ℃.
Example 2
380000Nm of flue gas of certain industrial kiln3The temperature of the flue gas is 150-350 ℃, and NO in the flue gasxThe concentration is 800mg/m3，SO2The concentration is 50mg/m3Dust concentration 10mg/m3。
(1) Determining the type of the catalyst according to the temperature range of the flue gas:
the first catalyst (medium-low temperature SCR catalyst) adopts a manganese-based catalyst, and the active temperature range of the manganese-based catalyst is 120-220 ℃; the second catalyst (medium-high temperature catalyst) adopts a high-vanadium catalyst (vanadium content is 3%), and the activity temperature range is 200-380 ℃;
(2) determining reactor parameters according to the amount of flue gas:
the reactor was arranged in 4 units (as shown in FIG. 2), with 6 catalyst modules per layer;
(3) determining the dosage of each catalyst according to the components of the flue gas:
the medium-low temperature catalyst has a diameter of 150X 1000mm and 25 holes, and the dosage is 19.4m3A unit;
the medium-high temperature catalyst is 150X 1200mm, has 30 holes, and has the dosage of 11.7m3A unit;
the total catalyst dosage is 124.3m3。
The denitration device and the denitration method provided by the embodiment of the invention are used for denitration of the flue gas, the denitration activity curve of the flue gas in a wide temperature range of 150-450 ℃ is shown in the attached drawing 3, as can be seen from the denitration curve shown in the attached drawing 3, the denitration efficiency of the flue gas at the temperature of 150 ℃ can reach 86%, and along with the improvement of the flue gas temperature, the denitration efficiency is increased to the highest point, and the denitration efficiency can reach 95%; along with the gradual rise of the flue gas temperature, the denitration efficiency is slightly reduced, but when the flue gas temperature is less than or equal to 350 ℃, the denitration efficiency is more than 85%, namely the denitration method and the denitration device can realize effective denitration within a wide temperature range of 150-350 ℃.
Example 3
The smoke quantity of an industrial kiln is 200000Nm3The temperature of the flue gas is 200-350 ℃, and NO in the flue gasxThe concentration is 400mg/m3，SO2The concentration is 100mg/m3Dust concentration 10g/m3。
(1) Determining the type of the catalyst according to the temperature range of the flue gas:
the first catalyst (medium-low temperature SCR catalyst) adopts a vanadium-based catalyst (vanadium content is 3%), and the active temperature range is 170-350 ℃; the second catalyst (medium-high temperature catalyst) adopts a low-vanadium catalyst (with vanadium content of 0.5%), and the activity temperature range is 300-400 ℃;
(2) determining reactor parameters according to the amount of flue gas:
the reactor was arranged in 4 units (as shown in FIG. 2), with 4 catalyst modules arranged in each layer;
(3) determining the dosage of each catalyst according to the components of the flue gas:
the medium-low temperature catalyst has a diameter of 150X 1000mm and 22 holes, and the dosage is 13.0m3A unit;
the medium-high temperature catalyst has a diameter of 150X 1200mm and 25 pores, and the dosage is 7.8m3A unit;
the total catalyst dosage is 83.2m3。
The denitration device and the denitration method provided by the embodiment of the invention are adopted to denitrate the flue gas, the denitration activity curve of the denitration device and the denitration method in a wide temperature range of 150-450 ℃ is shown in the attached drawing 3, the denitration efficiency of the denitration device can reach 70% at the temperature of 150 ℃ as seen from the denitration curve in the attached drawing 3, and the denitration efficiency of the denitration device and the denitration method can reach more than 90% when the temperature of the flue gas reaches 200 ℃ along with the improvement of the temperature of the flue gas; along with the rise of the temperature of the flue gas, the denitration efficiency is basically stabilized to be more than 90 percent; when the temperature of the flue gas exceeds 400 ℃, the denitration efficiency begins to be reduced, but can still reach more than 70%. From the foregoing, the denitration method and the denitration device of the embodiment can realize effective denitration within a wide temperature range of 200-400 ℃.
Example 4
The smoke gas amount of an industrial kiln is 350000Nm3The temperature of the flue gas is 150-300 ℃, and NO in the flue gasxThe concentration is 600mg/m3，SO2The concentration is 150mg/m3Dust concentration 5g/m3。
(1) Determining the type of the catalyst according to the temperature range of the flue gas:
the first catalyst (medium/low temperature SCR catalyst) adopts a manganese-based catalyst, and the activity temperature range of the manganese-based catalyst is 120-220 ℃; the second catalyst (medium/high temperature catalyst) adopts a high vanadium catalyst (vanadium content is 3.5%), and the active temperature range is 200-380 ℃;
(2) determining reactor parameters according to the amount of flue gas:
5 units are arranged in the reactor, 6 catalyst modules are arranged on each layer, and 1 unit is used as standby obstructed smoke in the operation process (5 units are used as standby units in turn);
(3) determining the dosage of each catalyst according to the components of the flue gas:
the medium-low temperature catalyst is 150X 1000mm with 18 holes and the dosage is19.4m3A unit;
the medium-high temperature catalyst has 150X 1100mm and 22 holes, and the dosage is 10.7m3A unit;
the total catalyst consumption is 150.5m3。
The denitration device and the denitration method provided by the embodiment of the invention are adopted to denitrate the flue gas, the denitration activity curve of the denitration device and the denitration method in a wide temperature range of 150-450 ℃ is shown in the attached drawing 3, the denitration efficiency of the denitration device at the temperature of 150 ℃ can reach 85% as seen from the denitration curve in the attached drawing 3, the denitration efficiency is increased to the highest point along with the increase of the flue gas temperature, and the denitration efficiency can reach 96%; along with the gradual rise of the flue gas temperature, the denitration efficiency is slightly reduced, but when the flue gas temperature is less than or equal to 350 ℃, the denitration efficiency is more than 87%, namely the denitration method and the denitration device can realize effective denitration within a wide temperature range of 150-300 ℃.
The features of the invention claimed and/or described in the specification may be combined, and are not limited to the combinations set forth in the claims by the recitations therein. The technical solutions obtained by combining the technical features in the claims and/or the specification also belong to the scope of the present invention.
The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention in any way, and any simple modification, equivalent change and modification made to the above embodiment according to the technical spirit of the present invention are still within the scope of the technical solution of the present invention.
Claims (15)
1. An SCR denitration method is characterized by comprising the following steps:
1) the flue gas passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in one direction to be denitrated; the temperature of the flue gas is 150-450 ℃;
2) the flue gas subjected to denitration in the step 1) is subjected to denitration by sequentially passing through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in a one-way mode;
wherein the activity temperature of the first catalyst is 120-350 ℃; the activity temperature of the second catalyst is 200-450 ℃.
2. The SCR denitration method according to claim 1, comprising the steps of:
1) the flue gas sequentially passes through the ceramic heat accumulator, the first catalyst, the reducing agent, the second catalyst, the first catalyst and the ceramic heat accumulator from bottom to top; the reducing agent is injected from bottom to top;
2) the flue gas after denitration in the step 1) sequentially passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator from top to bottom.
3. The SCR denitration method according to claim 1 or 2, further comprising injecting the flue gas with a reducing agent before step 1).
4. The SCR denitration method according to claim 1 or 2, further comprising a step of heating flue gas between step 1) and step 2).
5. The SCR denitration method according to claim 2 or 3, wherein the reducing agent is ammonia or urea.
6. The SCR denitration method according to claim 1 or 2, further comprising detecting the content of nitrogen oxides in the flue gas after step 2);
if the content of the nitrogen oxides is less than or equal to the set standard, the flue gas is discharged;
if the content of the nitrogen oxides is larger than the set standard, denitrating the flue gas according to the following steps A and B or steps A 'and B':
A. the flue gas passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in one direction to be denitrated;
B. b, the flue gas subjected to denitration in the step A is subjected to denitration by sequentially passing through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator in a one-way mode;
a', the flue gas sequentially passes through the ceramic heat accumulator, the first catalyst, the reducing agent, the second catalyst, the first catalyst and the ceramic heat accumulator from bottom to top; the reducing agent is injected from bottom to top;
b ', the flue gas subjected to denitration in the step A' sequentially passes through the ceramic heat accumulator, the first catalyst, the second catalyst, the first catalyst and the ceramic heat accumulator from top to bottom.
7. The SCR denitration method according to claim 1 or 2, wherein the first catalyst is selected from a vanadium-based catalyst and/or a manganese-based catalyst having a vanadium content of 2% or more; the second catalyst is selected from a vanadium-based catalyst and/or a vanadium-titanium catalyst with the vanadium content less than or equal to 3.5 percent.
8. An SCR denitration device, comprising:
the reactor comprises a plurality of reaction units which are arranged in parallel; each reaction unit is sequentially provided with a ceramic heat storage layer, a first catalyst bed layer, a second catalyst bed layer, a first catalyst bed layer and a ceramic heat storage layer from bottom to top; the tops of the reaction units are communicated with each other; the bottom of the reaction unit is provided with a flue gas input pipe and a flue gas output pipe; the flue gas input pipe and the flue gas output pipe are both provided with switches;
the flue gas input main pipe is respectively connected with the flue gas input pipes;
and the smoke output main pipe is respectively connected with the smoke output pipes.
9. The SCR denitration device according to claim 8, wherein the reaction unit is provided with a ceramic heat storage layer, a first catalyst bed layer, a reducing agent spray gun, a second catalyst bed layer, a first catalyst bed layer and a ceramic heat storage layer from bottom to top in sequence;
the SCR denitration device further includes:
a reductant storage tank;
one end of the reducing agent injection system is connected with the reducing agent storage tank, and the other end of the reducing agent injection system is connected with the reducing agent spray gun; a switch is arranged between the reducing agent injection system and the reducing agent spray gun; when the switch is turned on, the reducing agent spray gun can spray the reducing agent from bottom to top.
10. The SCR denitration device of claim 8, further comprising a reducing agent injection system; the reducing agent injection system is also connected with the flue gas input main pipe; a switch is arranged between the reducing agent injection system and the flue gas input main pipe; and when the switch is turned on, the reducing agent injection system can inject the reducing agent into the flue gas input manifold.
11. The SCR denitration device according to claim 9, wherein the ceramic heat storage layer, the first catalyst bed layer, the reducing agent spray gun, the second catalyst bed layer, the first catalyst bed layer, and the ceramic heat storage layer are detachably connected; and the relative distances among the ceramic heat storage layer, the first catalyst bed layer, the reducing agent spray gun, the second catalyst bed layer, the first catalyst bed layer and the ceramic heat storage layer can be adjusted.
12. The SCR denitration device according to any one of claims 8 to 11, further comprising a combustor; the burners are disposed in a region where the tops of the reaction units communicate with each other.
13. The SCR denitration device according to any one of claims 9 to 11, wherein in the reaction unit, when the switch of the flue gas input pipe is opened and the switch of the flue gas output pipe is closed, the reaction unit can move the flue gas from bottom to top, and the reaction unit at this time is defined as a type I reaction unit; when the switch of the flue gas input pipe is closed and the switch of the flue gas output pipe is opened, the reaction unit can enable the flue gas to move from top to bottom, and the reaction unit at the moment is defined as a II-type reaction unit;
and when the SCR denitration device works, the switch of the reducing agent spray gun in the I-type reaction unit is turned on, and the switch of the reducing agent spray gun in the II-type reaction unit is turned off.
14. The SCR denitration device of claim 13, wherein a flow direction of flue gas in the reaction unit can be changed by changing an on-off state of a flue gas input pipe and an on-off state of a flue gas output pipe of the reaction unit.
15. The SCR denitration device according to claim 13, wherein the number of the reaction units is 2 to 10.
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100322834A1 (en) * | 2006-04-13 | 2010-12-23 | Takehiko Ito | Method of and Apparatus for Treating Gas Containing Nitrous Oxide |
| DE102014106991A1 (en) * | 2013-05-27 | 2014-11-27 | Scheuch Gmbh | Device for catalytic denitrification and regenerative thermal afterburning |
| CN105536521A (en) * | 2016-01-12 | 2016-05-04 | 哈尔滨工业大学（威海） | Heat accumulating type oxidation device for catalysis denitration |
| US20170007990A1 (en) * | 2014-04-24 | 2017-01-12 | Tongji University | Honeycomb denitration catalyst for flue gas at 400°c-600°c and preparation method thereof |
| CN206064161U (en) * | 2016-08-24 | 2017-04-05 | 中电环保股份有限公司 | A kind of middle low-temperature denitration of flue gas device |
| CN107952363A (en) * | 2017-10-17 | 2018-04-24 | 上海交通大学 | A kind of low-temperature flue gas RT-SCR heat-storage catalytics reduction denitrating system and method |
| CN108159876A (en) * | 2017-12-26 | 2018-06-15 | 中国科学院过程工程研究所 | A kind of processing unit of sintering flue gas, method and purposes |
| CN108854530A (en) * | 2018-05-23 | 2018-11-23 | 清华大学盐城环境工程技术研发中心 | A kind of wide load SCR denitration device of middle low temperature and method of denitration |
| CN110605019A (en) * | 2019-10-18 | 2019-12-24 | 上海蓝科石化环保科技股份有限公司 | Treatment device and process integrating VOCs purification and denitration |
| CN210088885U (en) * | 2019-05-16 | 2020-02-18 | 青岛软控海科环保有限公司 | Two-bed heat-storage catalytic combustion system with high-efficiency treatment capacity |
-
2020
- 2020-12-31 CN CN202011637455.6A patent/CN112675702B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100322834A1 (en) * | 2006-04-13 | 2010-12-23 | Takehiko Ito | Method of and Apparatus for Treating Gas Containing Nitrous Oxide |
| DE102014106991A1 (en) * | 2013-05-27 | 2014-11-27 | Scheuch Gmbh | Device for catalytic denitrification and regenerative thermal afterburning |
| US20170007990A1 (en) * | 2014-04-24 | 2017-01-12 | Tongji University | Honeycomb denitration catalyst for flue gas at 400°c-600°c and preparation method thereof |
| CN105536521A (en) * | 2016-01-12 | 2016-05-04 | 哈尔滨工业大学（威海） | Heat accumulating type oxidation device for catalysis denitration |
| CN206064161U (en) * | 2016-08-24 | 2017-04-05 | 中电环保股份有限公司 | A kind of middle low-temperature denitration of flue gas device |
| CN107952363A (en) * | 2017-10-17 | 2018-04-24 | 上海交通大学 | A kind of low-temperature flue gas RT-SCR heat-storage catalytics reduction denitrating system and method |
| CN108159876A (en) * | 2017-12-26 | 2018-06-15 | 中国科学院过程工程研究所 | A kind of processing unit of sintering flue gas, method and purposes |
| CN108854530A (en) * | 2018-05-23 | 2018-11-23 | 清华大学盐城环境工程技术研发中心 | A kind of wide load SCR denitration device of middle low temperature and method of denitration |
| CN210088885U (en) * | 2019-05-16 | 2020-02-18 | 青岛软控海科环保有限公司 | Two-bed heat-storage catalytic combustion system with high-efficiency treatment capacity |
| CN110605019A (en) * | 2019-10-18 | 2019-12-24 | 上海蓝科石化环保科技股份有限公司 | Treatment device and process integrating VOCs purification and denitration |
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