CN212492357U - System for electron beam is in coordination with oxidant SOx/NOx control - Google Patents
System for electron beam is in coordination with oxidant SOx/NOx control Download PDFInfo
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Abstract
The utility model relates to a system for electron beam is oxidant SOx/NOx control in coordination, system for electron beam is oxidant SOx/NOx control in coordination includes gas-liquid mixing device, oxysulfide absorbing device, static mixer, nitrogen oxide absorbing device, oxidant feeding device, electron beam generating device, ammonia feeding device, absorption liquid feeding device, gas-liquid mixture injection apparatus and ozone generator and constitutes. The system firstly utilizes the oxidant provided by the oxidant supply device to treat the oxysulfide and the nitrogen oxide in the flue gas, firstly realizes the separation of the oxysulfide and the nitrogen oxide, then utilizes the electron beam generating device to carry out electron beam irradiation on excessive oxygen and water vapor, utilizes the generated strong oxidizing free radicals to oxidize the nitrogen oxide, and further realizes the treatment of the residual nitrogen oxide by matching with a small amount of ozone.
Description
Technical Field
The utility model belongs to the technical field of the flue gas is administered, a SOx/NOx control's system is related to, especially, relate to a system of oxidant SOx/NOx control is in coordination with to electron beam.
Background
Nitrogen oxide and sulfur dioxide are main pollutants in various types of flue gases, and when the nitrogen oxide and the sulfur dioxide are discharged into the atmosphere, the nitrogen oxide and the sulfur dioxide not only directly harm human health, but also cause a series of environmental problems such as haze, acid rain, photochemical smog and the like, so that the control of the discharge of the flue gases is of great importance for improving the quality of the atmospheric environment.
Mainstream technologies for flue gas desulfurization and denitration include wet flue gas desulfurization, SCR flue gas denitration, activated carbon/coke flue gas desulfurization and denitration, flue gas circulating fluidized bed desulfurization and denitration, and the like. The wet flue gas desulfurization mainly adopts limestone or lime-gypsum method, ammonia method, seawater desulfurization method and other methods. The limestone or lime-gypsum method is the most widely used wet flue gas desulfurization method, and has the advantages of high desulfurization efficiency, good operation reliability, wide absorbent source, low price and the like. SCR flue gas denitration technique has the denitration efficiency height, and area is little etc. advantage, but conventional SCR flue gas denitration technical requirement temperature is higher, and reaction temperature is low excessively not only influences denitration efficiency, and more importantly can make the catalyst poisoned.
In order to cope with industrial furnace flue gas with low temperature and complex components and places where an SCR denitration system is not suitable to be arranged, the technologies of activated carbon/coke flue gas desulfurization and denitration, flue gas circulating fluidized bed flue gas desulfurization and denitration and the like are popularized and applied in recent years. The activated carbon/coke flue gas desulfurization and denitrification technology has the advantages of purifying various pollutants, and has high purification efficiency, but the activated carbon/coke has higher cost and complex circulation and regeneration processes, so that the system failure rate is higher. The flue gas circulating fluidized bed technology has high purification efficiency, but the guarantee rate of the desulfurization efficiency is relatively low, and the problems of high system failure and the like are also faced. Based on this, an oxidation absorption method has been proposed.
The oxidation absorption method generally adopts ozone and/or hydrogen peroxide as an oxidant, the oxidation-reduction potential of the ozone is 2.07V, and the oxidability is second to that of hydroxyl radicals. In the oxidation process, oxygen atoms carried by ozone are consumed to enter a stable state, secondary pollution cannot be caused in the use process, but the problem of high denitration cost due to the use amount of ozone existing in the denitration by using ozone is solved; if the ozone dosage is reduced, NO in the flue gas is converted into NO more2Rather than higher valency N2O5Resulting in low efficiency of the subsequent absorption process. The oxydol has strong oxidizability, wide sources and low price, is reduced into water after the oxidation process, does not cause environmental pollution, is a green oxidant, but is also used for the denitrating of the oxydol at high temperature of about 500 ℃, has poor activity in the flue gas at low temperature (less than 280 ℃) and is not easy to utilize.
CN 205235751U discloses hydrogen peroxide solution oxidation denitration system, including the hydrogen peroxide solution holding vessel, the hydrogen peroxide solution holding vessel links to each other with the entry of hydrogen peroxide solution activation jar through the injection volume control appearance that links to each other with dynamic controller, the export of hydrogen peroxide solution activation jar links to each other with an entry of hybrid reactor, another entry of hybrid reactor links to each other with the boiler flue, the export links to each other with SOx/NOx control absorption tower bottom through the draught fan, the upper portion of SOx/NOx control absorption tower is equipped with spraying system, spraying system links to each other with an export in circulation pond, an entry in circulation pond links to each other with calcium hydroxide solution pond, another crossing links to each other with the bottom of SOx/NOx control absorption tower, another export links to each other with waste water treatment system, the flue gas outlet department of SOx/NOx control absorption tower isXA concentration monitor.
The hydrogen peroxide activation tank utilizes the high-temperature condition of the flue to ensure that H is generated2O2The hydroxyl free radical is generated by excitation, but the existence time of the hydroxyl free radical in the solution is short, the hydrogen peroxide is activated firstly, and then the hydrogen peroxide is contacted with the nitrogen oxide, so that the oxidation effect of the hydrogen peroxide is seriously weakened.
CN 106853327 a discloses a method and an apparatus for integrating desulfurization and denitrification with low temperature flue gas, wherein the apparatus integrates two or three of a plasma desulfurization and denitrification apparatus, a hydrogen peroxide catalytic activation desulfurization and denitrification apparatus and an ozone oxidation desulfurization and denitrification apparatus on a flue to be treated, in the scheme of the oil-containing plasma desulfurization and denitrification apparatus, the plasma desulfurization and denitrification apparatus is arranged at the foremost end of the flue, and under the condition that the hydrogen peroxide and ozone oxidation desulfurization and denitrification apparatus exist simultaneously, the hydrogen peroxide catalytic activation desulfurization and denitrification apparatus is positioned at the frontend. The device can utilize hydrogen peroxide, ozone and plasma to handle the flue gas in a flexible way, but does not have the cooperation effect between the three, and the consumption is still higher each other.
CN 106178863A discloses a desulfurization and denitrification method for boiler flue gas, which comprises the following steps: (1) preparing a desulfurization and denitrification agent; (2) treating the boiler flue gas with the desulfurization and denitrification agent obtained in the step (1) for 15-20min to obtain first desulfurization and denitrification flue gas; (3) carrying out heat exchange on the first desulfurization and denitration flue gas and the boiler flue gas to obtain cooled boiler flue gas and heated first desulfurization and denitration flue gas, then simultaneously carrying out ultraviolet irradiation and electron beam irradiation on the heated first desulfurization and denitration flue gas to obtain second desulfurization and denitration flue gas, and carrying out heat exchange on the second desulfurization and denitration flue gas and the cooled boiler flue gas to obtain cooled second desulfurization and denitration flue gas and heated boiler flue gas; (4) and (4) treating the secondary desulfurization and denitrification flue gas obtained in the step (3) by water spraying. The method needs to use ultraviolet irradiation and electron beam irradiation simultaneously, so that the energy consumption is high, and the temperature of the desulfurization and denitrification flue gas is high.
To this, the utility model provides an utilize electron beam in coordination with oxidant SOx/NOx control's system, the system utilizes electron beam irradiation to produce the stronger free radical of oxidability, combines the effect of oxidant to accomplish the oxidation absorption to sulfur oxide and nitrogen oxide in the flue gas simultaneously, has realized the purpose that SOx/NOx control energy consumption reduces.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a system of electron beam cooperation oxidant SOx/NOx control, the system can make full use of the oxidant oxidize nitrogen oxide and oxysulfide in to the flue gas, and can fully get rid of nitrogen oxide and oxysulfide in the flue gas.
In order to achieve the purpose of the utility model, the utility model adopts the following technical proposal:
the utility model provides a system for electron beam is oxidant SOx/NOx control in coordination, the system is including the gas-liquid mixing device, oxysulfide absorbing device, static mixer and the nitrogen oxide absorbing device that set gradually.
The flue gas and the oxidant provided by the oxidant supply device flow into the oxysulfide absorption device after being mixed in the gas-liquid mixing device.
And the tail end of the static mixer is provided with an electron beam generating device, and gas discharged by the oxysulfide absorbing device is mixed with ammonia gas provided by the ammonia supply device in the static mixer and flows into the nitric oxide absorbing device after flowing through the electron beam generating device.
And the side wall of the nitrogen oxide absorption device is provided with a gas-liquid mixing and spraying device, and the gas-liquid mixing and spraying device is used for spraying the absorption liquid provided by the absorption liquid supply device and the ozone provided by the ozone generating device into the nitrogen oxide absorption device together by the gas-liquid mixing and spraying device.
The absorption liquid supply device comprises but is not limited to an absorption liquid storage tank and a delivery pump for delivering the absorption liquid; the gas-liquid mixing device is a conventional gas-liquid mixer; the oxidant supply device comprises but is not limited to an oxidant storage tank and a delivery pump for delivering the oxidant; the oxysulfide absorbing device is a spray tower; the ammonia supply device is a conventional ammonia supply device; the electron beam generating device is a conventional electron beam generator for mixing O in ammonia gas2And H2O is converted into a large amount of OH and O radicalsRadicals, these radicals and SO in flue gases2And nitrogen oxide to generate H at a very fast speed2SO4And HNO3，H2SO4And HNO3Reacting with ammonia gas to generate by-products of ammonium nitrate and ammonium sulfate; the nitrogen oxide absorption device is a spray tower; the ozone generating device includes but is not limited to an ozone generator; the gas-liquid mixing and spraying device is a conventional gas-liquid mixing sprayer in the field, and only needs to realize the co-spraying of the absorption liquid and the ozone.
When the system provided by the utility model is used for desulfurization and denitrification, the flue gas and the oxidant are mixed in the gas-liquid mixing device, most of oxysulfide and nitric oxide in the flue gas are oxidized by using the oxidation effect of the oxidant, and then the desulfurizer in the oxysulfide absorbing device is used for absorbing the oxysulfide; o produced by excess oxidant2And H2The O flows into a static mixer along with the desulfurization gas, is uniformly mixed with ammonia gas at the front end of the static mixer, and is irradiated by an electron beam generating device to ensure that the O2And H2O is converted into a large amount of OH and O free radicals which are combined with SO in the flue gas2And nitrogen oxide to generate H at a very fast speed2SO4And HNO3，H2SO4And HNO3The residual activated gas is oxidized and absorbed by a small amount of ozone and absorption liquid introduced into the nitrogen oxide absorption device, the contents of the nitrogen oxide and the sulfur oxide in the obtained purified gas are low, and the oxidant is fully utilized.
Preferably, the system further comprises a heat exchange device, wherein the heat exchange device is used for exchanging heat between the absorption liquid provided by the absorption liquid supply device and the flue gas; the heat exchange device is a heat exchanger conventional in the field, and comprises a shell-and-tube heat exchanger and/or a dividing wall type heat exchanger.
Mixing the heat-exchanged flue gas with an oxidant provided by an oxidant supply device in a gas-liquid mixing device; the absorption liquid after heat exchange and ozone provided by the ozone generating device are sprayed into the nitrogen oxide absorption device by the gas-liquid mixing and spraying device.
The flue gas is subjected to heat exchange, so that the temperature of the flue gas meets the reaction requirement when the flue gas reacts with hydrogen peroxide, and the flue gas is oxidized at the heat exchange temperature, so that the removal rate of sulfur oxides in the flue gas can be improved, and the flue gas can be preheated for utilization.
Preferably, the side wall of the nitrogen oxide absorption device is provided with 1-3 gas-liquid mixing injection devices, for example, 1, 2 or 3, and the side wall of the nitrogen oxide absorption device is provided with 2 gas-liquid mixing injection devices, considering the nitrogen oxide removal rate and the operation difficulty.
Preferably, the 2 gas-liquid mixing and spraying devices are arranged on the side wall of the desulfurization and denitrification reactor in an up-down relationship, and a discharge hole of the gas-liquid mixing and spraying device positioned at the bottom is arranged opposite to an air inlet of the nitrogen oxide absorption device; the air inlet is used for being connected with an air outlet of the static mixer.
Use the utility model provides a system of electron beam in coordination with oxidant SOx/NOx control carries out SOx/NOx control's method to the flue gas includes following step:
(1) mixing flue gas and an oxidant, and treating the mixture by using a desulfurizer to obtain desulfurized gas;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas to obtain activated gas;
(3) and (3) spraying ozone and absorption liquid into a nitrogen oxide absorption device together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid.
Preferably, the flow rate of the flue gas in the step (1) is 50-80Nm3Is, for example, 50Nm3/s、55Nm3/s、60Nm3/s、65Nm3/s、70Nm3/s、75Nm3/s or 80Nm3And/s, but not limited to the recited values, other values within the range of values not recited are equally applicable.
Preferably, SO in the flue gas in the step (1)2The mass concentration of the active carbon is 500-800mg/Nm3For example, it may be 500mg/Nm3、550mg/Nm3、600mg/Nm3、650mg/Nm3、700mg/Nm3、750mg/Nm3Or 800mg/Nm3But are not limited to the recited values, other values not recited within the numerical range are equally applicable; the mass concentration of nitrogen oxide is less than or equal to 300mg/Nm3For example, it may be 150mg/Nm3、180mg/Nm3、200mg/Nm3、210mg/Nm3、240mg/Nm3、250mg/Nm3、270mg/Nm3、280mg/Nm3Or 300mg/Nm3But are not limited to the recited values, and other values within the numerical range not recited are equally applicable.
Preferably, the oxidant in the step (1) is hydrogen peroxide.
Preferably, the hydrogen peroxide and SO in the flue gas2The molar ratio of (1.5-2.5):1, for example 1.5:1, 1.8:1, 2:1, 2.2:1 or 2.5:1, but is not limited to the values listed, and other values not listed in the numerical range are equally applicable.
Preferably, the desulfurizing agent in step (1) is an alkaline solution with a pH value of 7.5-11, the pH value of the alkaline solution is 7.5-11, for example, 7.5, 8, 8.5, 9, 9.5, 10, 10.5 or 11, but not limited to the enumerated values, and other unrecited values in the numerical range are also applicable.
Preferably, the alkaline substance in the alkaline solution comprises any one or a combination of at least two of sodium hydroxide, ammonia, magnesium hydroxide or calcium hydroxide, typical but non-limiting combinations include a combination of sodium hydroxide and ammonia, a combination of ammonia and magnesium hydroxide, a combination of magnesium hydroxide and calcium hydroxide, a combination of sodium hydroxide, ammonia and magnesium hydroxide, a combination of ammonia, magnesium hydroxide and calcium hydroxide, or a combination of sodium hydroxide, ammonia, magnesium hydroxide and calcium hydroxide; calcium hydroxide is preferred.
Preferably, the molar ratio of ammonia gas in step (2) to oxidant in step (1) is (0.3-0.8):1, and may be, for example, 0.3:1, 0.4:1, 0.5:1, 0.6:1, 0.7:1 or 0.8:1, but is not limited to the recited values, and other values not recited within the numerical range are equally applicable.
Preferably, the temperature of the electron beam irradiation in step (2) is 50 to 70 ℃, for example, 50 ℃, 55 ℃, 60 ℃, 65 ℃ or 70 ℃, but not limited to the recited values, and other values not recited in the numerical range are also applicable.
Preferably, the liquid-gas ratio of the absorption liquid to the activated gas in the step (3) is 5-10L/Nm3For example, it may be 5L/Nm3、6L/Nm3、7L/Nm3、8L/Nm3、9L/Nm3Or 10L/Nm3But are not limited to the recited values, and other values within the numerical range not recited are equally applicable.
Preferably, the molar ratio of ozone to NO in the flue gas in step (3) is (0.2-0.4):1, and may be, for example, 0.2:1, 0.25:1, 0.3:1, 0.35:1 or 0.4:1, but is not limited to the values recited, and other values not recited in the range of values are equally applicable.
Preferably, the absorption liquid in step (3) is an alkaline solution with a pH value of 7.5-10, the pH value of the alkaline solution is 7.5-10, for example, 7.5, 8, 8.5, 9, 9.5 or 10, but not limited to the recited values, and other values not recited in the numerical range are also applicable; the alkaline substance in the alkaline solution comprises any one or a combination of at least two of sodium hydroxide, ammonia water, calcium hydroxide or magnesium hydroxide, and typical but non-limiting combinations comprise a combination of sodium hydroxide and ammonia water, a combination of ammonia water and magnesium hydroxide, a combination of magnesium hydroxide and calcium hydroxide, a combination of sodium hydroxide, ammonia water and magnesium hydroxide, a combination of ammonia water, magnesium hydroxide and calcium hydroxide, or a combination of sodium hydroxide, ammonia water, magnesium hydroxide and calcium hydroxide; calcium hydroxide is preferred.
Preferably, the ozone and the absorption liquid in step (3) are respectively and independently divided into at least two, preferably two, streams.
Preferably, in the step (3), the ozone is divided into ozone I and ozone II, the absorption liquid is divided into absorption liquid I and absorption liquid II, the ozone I and the absorption liquid I are mixed and sprayed into the nitrogen oxide absorption device, the ozone II and the absorption liquid II are mixed and sprayed into the desulfurization and denitrification reactor, and the spraying port of the ozone I is located below the spraying port of the ozone II.
Preferably, the flow ratio of ozone I to ozone II is (2-5):1, and can be, for example, 2:1, 2.5:1, 3:1, 3.5:1, 4:1, 4.5:1 or 5:1, but is not limited to the recited values, and other values not recited in the numerical ranges are equally applicable; the flow ratio of the absorbing solution I to the absorbing solution II is (1-2): 1-2, and may be, for example, 1:1, 1:1.5, 1:2, 2:1.5 or 2:1, but is not limited to the values listed, and other values not listed in the numerical range are also applicable.
Preferably, the method further comprises the step of exchanging heat between the flue gas and the absorption liquid before the step (1);
preferably, the temperature of the flue gas after heat exchange is reduced to 100-150 ℃, for example, 100 ℃, 110 ℃, 120 ℃, 130 ℃, 140 ℃ or 150 ℃, but not limited to the recited values, and other values not recited in the numerical range are also applicable.
The system refers to an equipment system, or a production equipment.
As a preferable technical scheme of the method, the method comprises the following steps:
(1) the flue gas and the absorption liquid exchange heat to reduce the temperature of the flue gas to 100-150 ℃, the flue gas and hydrogen peroxide are mixed, and the mixture is treated by a desulfurizer to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2The molar ratio of (1.5-2.5) to (1); the desulfurizer is an alkaline solution with the pH value of 7.5-11;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 50-70 ℃ to obtain activated gas; the molar ratio of the ammonia gas to the hydrogen peroxide in the step (1) is (0.3-0.8) to 1;
(3) spraying ozone and absorption liquid into a nitrogen oxide absorption device together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 5-10L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is (0.2-0.4) to 1; the absorption liquid is alkaline solution with pH value of 7.5-10.
Further preferably, the method comprises the steps of:
(1) the flue gas and the absorption liquid exchange heat to reduce the temperature of the flue gas to 100-150 ℃, and the mixed flue gas and the hydrogen peroxide solution areTreating the mixture by a desulfurizing agent to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2The molar ratio of (1.5-2.5) to (1); the desulfurizer is an alkaline solution with the pH value of 7.5-11;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 50-70 ℃ to obtain activated gas; the molar ratio of the ammonia gas to the hydrogen peroxide in the step (1) is (0.3-0.8) to 1;
(3) the ozone is divided into ozone I and ozone II, the absorption liquid is divided into absorption liquid I and absorption liquid II, the ozone I and the absorption liquid I are mixed and sprayed into the nitrogen oxide absorption device, the ozone II and the absorption liquid II are mixed and sprayed into the desulfurization and denitrification reactor, and the spraying port of the ozone I is positioned below the spraying port of the ozone II; the flow ratio of the ozone I to the ozone II is (2-5) to 1, and the flow ratio of the absorption liquid I to the absorption liquid II is (1-2) to (1-2); spraying ozone and absorption liquid into a nitrogen oxide absorption device together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 5-10L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is (0.2-0.4) to 1; the absorption liquid is alkaline solution with pH value of 7.5-10.
Compared with the prior art, the utility model discloses following beneficial effect has:
the system firstly utilizes the oxidant provided by the oxidant supply device to treat the oxysulfide and the nitrogen oxide in the flue gas, firstly realizes the separation of the oxysulfide and the nitrogen oxide, then utilizes the electron beam generating device to carry out electron beam irradiation on excessive oxygen and water vapor, utilizes the generated strong oxidizing free radical to oxidize the nitrogen oxide, and further cooperates with a small amount of ozone to realize the treatment of the residual nitrogen oxide, and finally, SO in the flue gas2The removal rate of the nitrogen oxide can reach 99.9 percent, and the removal rate of the nitrogen oxide can reach 97.7 percent.
Drawings
FIG. 1 is a schematic structural diagram of a system for desulfurization and denitrification with electron beam and oxidant provided in example 1;
FIG. 2 is a schematic structural diagram of a system for desulfurization and denitrification with electron beam and oxidant provided in example 2;
fig. 3 is a schematic structural diagram of a system for desulfurization and denitrification with electron beam in cooperation with an oxidant provided in example 3.
Wherein: 1, an absorption liquid supply device; 2, a heat exchange device; 3, a gas-liquid mixing device; 4, an oxidant supply device; 5, a sulfur oxide absorption device; 6, an ammonia supply device; 7, a static mixer; 71, an electron beam generating device; 8, a nitrogen oxide absorption device; 9, an ozone generating device; and 91, a gas-liquid mixing and injecting device.
Detailed Description
The technical solution of the present invention will be further explained by the following embodiments. It should be understood by those skilled in the art that the described embodiments are merely provided to assist in understanding the present invention and should not be construed as specifically limiting the present invention.
Example 1
The present embodiment provides a system for desulfurization and denitrification with an electron beam in cooperation with an oxidant, the structural schematic diagram of the system is shown in fig. 1, and the system includes a gas-liquid mixing device 3, a sulfur oxide absorption device 5, a static mixer 7 and a nitrogen oxide absorption device 8, which are sequentially arranged;
the flue gas and the oxidant supplied by the oxidant supply device 4 are mixed in the gas-liquid mixing device 3 and then flow into the oxysulfide absorption device 5; an electron beam generating device 71 is arranged at the tail end of the static mixer 7, the gas discharged by the oxysulfide absorbing device 5 is mixed with the ammonia gas supplied by the ammonia supply device 6 in the static mixer 7, and flows into the nitrogen oxide absorbing device 8 after flowing through the electron beam generating device 71; the side wall of the nitrogen oxide absorption device 8 is provided with 1 gas-liquid mixing injection device 91, the gas-liquid mixing injection device 91 is used for injecting the absorption liquid provided by the absorption liquid supply device 1 and the ozone provided by the ozone generation device 9 into the nitrogen oxide absorption device 8 together through the gas-liquid mixing injection device 91, and the discharge hole of the gas-liquid mixing injection device 91 is opposite to the air inlet of the nitrogen oxide absorption device 8; the gas inlet is used for being connected with the gas outlet of the static mixer 7.
The absorption liquid supply device 1 includes an absorption liquid storage tank and a transfer pump for transferring the absorption liquid; the oxidant supply means 4 comprises an oxidantThe oxysulfide absorbing device 5 is a spray tower and comprises a storage tank and a delivery pump for delivering an oxidant; the ammonia supply device 6 is a conventional ammonia supply device; the electron beam generating device 71 is a conventional electron beam generator for mixing O in ammonia gas2And H2O is converted into a large amount of OH and O free radicals; the nitrogen oxide absorption device 8 is a spray tower; the ozone generating device 9 is an ozone generator; the gas-liquid mixing and injecting device 91 is a gas-liquid mixing injector conventional in the art.
When the system provided by the embodiment is used for desulfurization and denitrification, flue gas and an oxidant are mixed in the gas-liquid mixing device 3, most of sulfur oxides and nitrogen oxides in the flue gas are oxidized by the oxidation action of the oxidant, and then the sulfur oxides are absorbed by a desulfurizer in the sulfur oxide absorption device 5; o produced by excess oxidant2And H2The O flows into the static mixer 7 along with the desulfurization gas, is uniformly mixed with the ammonia gas at the front end of the static mixer 7, and is irradiated by the electron beam generating device 71 to ensure that the O2And H2O is converted into a large amount of OH and O free radicals which are combined with SO in the flue gas2And nitrogen oxide to generate H at a very fast speed2SO4And HNO3，H2SO4And HNO3The ammonia gas reacts to generate by-products of ammonium nitrate and ammonium sulfate, the nitrogen oxides and the sulfur oxides in the residual activated gas are oxidized and absorbed by a small amount of ozone and absorption liquid introduced into the nitrogen oxide absorption device 8, the contents of the nitrogen oxides and the sulfur oxides in the obtained purified gas are low, and the oxidant is fully utilized.
Example 2
The embodiment provides a system for desulfurization and denitrification by electron beam in cooperation with an oxidant, the structural schematic diagram of the system is shown in fig. 2, and compared with embodiment 1, the system is further provided with a heat exchange device 2.
The heat exchange device 2 is used for exchanging heat between the absorption liquid provided by the absorption liquid supply device 1 and the flue gas, and the flue gas after heat exchange is mixed with the oxidant provided by the oxidant supply device 4 in the gas-liquid mixing device 3; the absorption liquid after heat exchange and ozone provided by the ozone generator 9 are sprayed into the nitrogen oxide absorption device 8 by the gas-liquid mixing and spraying device 91.
This embodiment passes through heat transfer device 2's setting, makes flue gas and absorption liquid carry out the heat transfer, has not only utilized the waste heat of flue gas, can also make the flue gas reduce to the suitable temperature when acting on with hydrogen peroxide to make the absorption liquid intensification in order to promote ozone oxidation to absorb in coordination.
When the system provided by the embodiment is used for desulfurization and denitrification, the flue gas and the absorption liquid provided by the absorption liquid supply device 1 exchange heat in the heat exchange device 2, then the flue gas and the oxidant are mixed in the gas-liquid mixing device 3, most of sulfur oxides and nitrogen oxides in the flue gas are oxidized by the oxidation action of the oxidant, and then the sulfur oxides are absorbed by the desulfurizer in the sulfur oxide absorption device 5; o produced by excess oxidant2And H2The O flows into the static mixer 7 along with the desulfurization gas, is uniformly mixed with the ammonia gas at the front end of the static mixer 7, and is irradiated by the electron beam generating device 71 to ensure that the O2And H2O is converted into a large amount of OH and O free radicals which are combined with SO in the flue gas2And nitrogen oxide to generate H at a very fast speed2SO4And HNO3，H2SO4And HNO3The ammonia gas reacts to generate by-products of ammonium nitrate and ammonium sulfate, the nitrogen oxides and the sulfur oxides in the residual activated gas are oxidized and absorbed by a small amount of ozone and absorption liquid introduced into the nitrogen oxide absorption device 8, the contents of the nitrogen oxides and the sulfur oxides in the obtained purified gas are low, and the oxidant is fully utilized.
Example 3
The present embodiment provides a system for desulfurization and denitrification with an electron beam in cooperation with an oxidant, the structural schematic diagram of the system is as shown in fig. 3, and compared with embodiment 2, except that 2 gas-liquid mixing injection devices 91 are arranged on the side wall of a nitrogen oxide absorption device 8 in the system, the 2 gas-liquid mixing injection devices 91 are arranged on the side wall of a desulfurization and denitrification reactor in an up-down relationship, the discharge port of the gas-liquid mixing injection device 91 at the bottom is arranged opposite to the gas inlet of the nitrogen oxide absorption device 8, and the gas inlet is used for being connected with the gas outlet of a static mixer 7, the rest is the same as embodiment 2.
When the system provided by the embodiment is used for desulfurization and denitrification, the flue gas and the absorption liquid provided by the absorption liquid supply device 1 exchange heat in the heat exchange device 2, then the flue gas and the oxidant are mixed in the gas-liquid mixing device 3, most of sulfur oxides and nitrogen oxides in the flue gas are oxidized by the oxidation action of the oxidant, and then the sulfur oxides are absorbed by the desulfurizer in the sulfur oxide absorption device 5; o produced by excess oxidant2And H2The O flows into the static mixer 7 along with the desulfurization gas, is uniformly mixed with the ammonia gas at the front end of the static mixer 7, and is irradiated by the electron beam generating device 71 to ensure that the O2And H2O is converted into a large amount of OH and O free radicals which are combined with SO in the flue gas2And nitrogen oxide to generate H at a very fast speed2SO4And HNO3，H2SO4And HNO3The ammonia gas reacts to generate by-products of ammonium nitrate and ammonium sulfate, the nitrogen oxides and the sulfur oxides in the residual activated gas are oxidized and absorbed by a small amount of ozone and absorption liquid introduced into the nitrogen oxide absorption device 8, the contents of the nitrogen oxides and the sulfur oxides in the obtained purified gas are low, and the oxidant is fully utilized.
Ozone that lets in nitrogen oxide absorbing device 8 is divided into ozone I and ozone II, the absorption liquid is divided into absorption liquid I and absorption liquid II, and ozone I mixes with absorption liquid I and spouts into nitrogen oxide absorbing device 8, and ozone II mixes with absorption liquid II and spouts into SOx/NOx control reactor, and ozone I's the mouth of spouting is located ozone II and spouts the below of mouth.
By dividing the ozone and the absorption liquid into two parts, the ozone utilization rate is improved when the ozone oxidizes the residual nitrogen oxides, and the content of the nitrogen oxides and the sulfur oxides in the finally obtained purified gas is further reduced.
Application example
Use the embodiment of the utility model provides a system carries out SOx/NOx control to the flue gas and handles, unified test condition, the flue gas is the dust removal back volume flue gas, and the flow is 80Nm3S and flue gasIn SO2Has a mass concentration of 800mg/Nm3The mass concentration of nitrogen oxide is 300mg/Nm3The temperature of the flue gas is controlled to make the temperature of the flue gas flowing into the gas-liquid mixing device 3 be 100-150 ℃.
Application example 1
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in embodiment 1, and the method includes the following steps:
(1) mixing hydrogen peroxide and flue gas at 120 ℃, and treating the mixture by using a desulfurizing agent to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 2: 1; the desulfurizer is calcium hydroxide solution with the pH value of 9;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 60 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.5: 1;
(3) spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 8L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.3: 1; the absorption liquid is calcium hydroxide solution with pH value of 9.
Application example 2
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in embodiment 1, and the method includes the following steps:
(1) mixing hydrogen peroxide and the flue gas at the temperature of 110 ℃, and treating the mixture by using a desulfurizing agent to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 1.8: 1; the desulfurizer is calcium hydroxide solution with the pH value of 10;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 65 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.4: 1;
(3) spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid(ii) a The liquid-gas ratio of the absorption liquid to the activated gas is 9L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.35: 1; the absorption liquid is calcium hydroxide solution with pH value of 8.
Application example 3
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in embodiment 1, and the method includes the following steps:
(1) mixing hydrogen peroxide and flue gas at 140 ℃, and treating the mixture by using a desulfurizing agent to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 2.2: 1; the desulfurizer is a sodium hydroxide solution with the pH value of 8;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 55 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.7: 1;
(3) spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 6L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.25: 1; the absorption liquid is sodium hydroxide solution with pH value of 9.5.
Application example 4
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in embodiment 1, and the method includes the following steps:
(1) mixing hydrogen peroxide with flue gas at 100 ℃, and treating the mixture by using a desulfurizing agent to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 1.5: 1; the desulfurizer is a sodium hydroxide solution with the pH value of 11;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 50 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.8: 1;
(3) spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the absorption liquid and the active ingredientsThe liquid-gas ratio of the liquefied gas is 10L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.4: 1; the absorption liquid is sodium hydroxide solution with pH value of 7.5.
Application example 5
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in embodiment 1, and the method includes the following steps:
(1) mixing hydrogen peroxide and flue gas at 150 ℃, and treating the mixture by using a desulfurizing agent to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 2.5: 1; the desulfurizer is calcium hydroxide solution with the pH value of 7.5;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 70 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.3: 1;
(3) spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 5L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.2: 1; the absorption liquid is sodium hydroxide solution with pH value of 10.
Application example 6
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in the embodiment 2, and the method comprises the following steps:
(1) the flue gas and the absorption liquid exchange heat to reduce the temperature of the flue gas to 120 ℃, hydrogen peroxide and the flue gas are mixed, and the mixture is treated by a desulfurizer to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 2: 1; the desulfurizer is calcium hydroxide solution with the pH value of 9;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 60 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.5: 1;
(3) spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorption liquidCollecting the liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 8L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.3: 1; the absorption liquid is calcium hydroxide solution with pH value of 9.
Compared with the application example 1, the heat exchange device 2 is used for exchanging heat between the flue gas and the absorption liquid, so that the waste heat of the flue gas is utilized, the flue gas can be reduced to a proper temperature when acting with hydrogen peroxide, and the absorption liquid is heated to promote ozone oxidation and synergistic absorption.
Application example 7
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in the embodiment 2, and the method comprises the following steps:
(1) the flue gas and the absorption liquid exchange heat to reduce the temperature of the flue gas to 110 ℃, hydrogen peroxide and the flue gas are mixed, and the mixture is treated by a desulfurizer to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 1.8: 1; the desulfurizer is calcium hydroxide solution with the pH value of 10;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 65 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.4: 1;
(3) spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 9L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.35: 1; the absorption liquid is calcium hydroxide solution with pH value of 8.
Compared with the application example 2, the heat exchange device 2 is used for exchanging heat between the flue gas and the absorption liquid, so that the waste heat of the flue gas is utilized, the flue gas can be reduced to a proper temperature when acting with hydrogen peroxide, and the absorption liquid is heated to promote ozone oxidation and synergistic absorption.
Application example 8
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in the embodiment 2, and the method comprises the following steps:
(1) the flue gas and the absorption liquid exchange heat to reduce the temperature of the flue gas to 140 ℃, hydrogen peroxide and the flue gas are mixed, and the mixture is treated by a desulfurizer to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 2.2: 1; the desulfurizer is a sodium hydroxide solution with the pH value of 8;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 55 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.7: 1;
(3) spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 6L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.25: 1; the absorption liquid is sodium hydroxide solution with pH value of 9.5.
Compared with the application example 3, the heat exchange device 2 is used for exchanging heat between the flue gas and the absorption liquid, so that the waste heat of the flue gas is utilized, the flue gas can be reduced to a proper temperature when acting with hydrogen peroxide, and the temperature of the absorption liquid is increased to promote ozone oxidation and synergistic absorption.
Application example 9
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in embodiment 1, and the method includes the following steps:
(1) the flue gas and the absorption liquid exchange heat to reduce the temperature of the flue gas to 100 ℃, hydrogen peroxide and the flue gas are mixed, and the mixture is treated by a desulfurizer to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 1.5: 1; the desulfurizer is a sodium hydroxide solution with the pH value of 11;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 50 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.8: 1;
(3) spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbPost-liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 10L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.4: 1; the absorption liquid is sodium hydroxide solution with pH value of 7.5.
Compared with the application example 4, the heat exchange device 2 is used for exchanging heat between the flue gas and the absorption liquid, so that the waste heat of the flue gas is utilized, the flue gas can be reduced to a proper temperature when acting with hydrogen peroxide, and the temperature of the absorption liquid is increased to promote ozone oxidation and synergistic absorption.
Application example 10
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in the embodiment 2, and the method comprises the following steps:
(1) the flue gas and the absorption liquid exchange heat to reduce the temperature of the flue gas to 150 ℃, hydrogen peroxide and the flue gas are mixed, and the mixture is treated by a desulfurizer to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 2.5: 1; the desulfurizer is calcium hydroxide solution with the pH value of 7.5;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 70 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.3: 1;
(3) spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 5L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.2: 1; the absorption liquid is sodium hydroxide solution with pH value of 10.
Compared with the application example 5, the heat exchange device 2 is used for exchanging heat between the flue gas and the absorption liquid, so that the waste heat of the flue gas is utilized, the flue gas can be reduced to a proper temperature when acting with hydrogen peroxide, and the temperature of the absorption liquid is increased to promote ozone oxidation and synergistic absorption.
Application example 11
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in the embodiment 3, and the method comprises the following steps:
(1) the flue gas and the absorption liquid exchange heat to reduce the temperature of the flue gas to 120 ℃, the flue gas and hydrogen peroxide are mixed, and the mixture is treated by a desulfurizer to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 2: 1; the desulfurizer is calcium hydroxide solution with the pH value of 9;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 60 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.5: 1;
(3) the ozone is divided into ozone I and ozone II, the absorption liquid is divided into absorption liquid I and absorption liquid II, the ozone I and the absorption liquid I are mixed and sprayed into a nitrogen oxide absorption device 8, the ozone II and the absorption liquid II are mixed and sprayed into the desulfurization and denitrification reactor, and the spraying port of the ozone I is positioned below the spraying port of the ozone II; the flow ratio of the ozone I to the ozone II is 3.5:1, and the flow ratio of the absorption liquid I to the absorption liquid II is 2: 1; spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 8L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.3: 1; the absorption liquid is calcium hydroxide solution with pH value of 9.
Application example 12
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in the embodiment 3, and the method comprises the following steps:
(1) the flue gas and the absorption liquid exchange heat to reduce the temperature of the flue gas to 110 ℃, the flue gas and hydrogen peroxide are mixed, and the mixture is treated by a desulfurizer to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 1.8: 1; the desulfurizer is calcium hydroxide solution with the pH value of 10;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 65 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.4: 1;
(3) ozone is divided into ozone I and ozone II, and absorption liquid is divided into absorption liquid I and absorption liquid IIMixing oxygen I and absorption liquid I and spraying the mixture into a nitrogen oxide absorption device 8, mixing ozone II and absorption liquid II and spraying the mixture into a desulfurization and denitrification reactor, wherein the spraying inlet of the ozone I is positioned below the spraying inlet of the ozone II; the flow ratio of the ozone I to the ozone II is 3:1, and the flow ratio of the absorption liquid I to the absorption liquid II is 2: 1.5; spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 9L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.35: 1; the absorption liquid is calcium hydroxide solution with pH value of 8.
Application example 13
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in the embodiment 3, and the method comprises the following steps:
(1) the flue gas and the absorption liquid exchange heat to reduce the temperature of the flue gas to 140 ℃, the flue gas and hydrogen peroxide are mixed, and the mixture is treated by a desulfurizer to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 2.2: 1; the desulfurizer is a sodium hydroxide solution with the pH value of 8;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 55 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.7: 1;
(3) the ozone is divided into ozone I and ozone II, the absorption liquid is divided into absorption liquid I and absorption liquid II, the ozone I and the absorption liquid I are mixed and sprayed into a nitrogen oxide absorption device 8, the ozone II and the absorption liquid II are mixed and sprayed into the desulfurization and denitrification reactor, and the spraying port of the ozone I is positioned below the spraying port of the ozone II; the flow ratio of the ozone I to the ozone II is 2:1, and the flow ratio of the absorption liquid I to the absorption liquid II is 1: 1; spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 6L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.25: 1; the absorption liquid is sodium hydroxide solution with pH value of 9.5.
Application example 14
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in the embodiment 3, and the method comprises the following steps:
(1) the flue gas and the absorption liquid exchange heat to reduce the temperature of the flue gas to 100 ℃, the flue gas and hydrogen peroxide are mixed, and the mixture is treated by a desulfurizer to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 1.5: 1; the desulfurizer is a sodium hydroxide solution with the pH value of 11;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 50 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.8: 1;
(3) the ozone is divided into ozone I and ozone II, the absorption liquid is divided into absorption liquid I and absorption liquid II, the ozone I and the absorption liquid I are mixed and sprayed into a nitrogen oxide absorption device 8, the ozone II and the absorption liquid II are mixed and sprayed into the desulfurization and denitrification reactor, and the spraying port of the ozone I is positioned below the spraying port of the ozone II; the flow ratio of the ozone I to the ozone II is 4:1, and the flow ratio of the absorption liquid I to the absorption liquid II is 1: 1.5; spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 10L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.4: 1; the absorption liquid is sodium hydroxide solution with pH value of 7.5.
Application example 15
The application example provides a method for performing desulfurization and denitrification on flue gas by using the system provided in the embodiment 3, and the method comprises the following steps:
(1) the flue gas and the absorption liquid exchange heat to reduce the temperature of the flue gas to 150 ℃, the flue gas and hydrogen peroxide are mixed, and the mixture is treated by a desulfurizer to obtain desulfurized gas; the hydrogen peroxide and SO in the flue gas2In a molar ratio of 2.5: 1; the desulfurizer is calcium hydroxide solution with the pH value of 7.5;
(2) mixing ammonia gas with the desulfurized gas obtained in the step (1) to obtain ammonia mixed gas, and performing electron beam irradiation on the obtained ammonia mixed gas at 70 ℃ to obtain activated gas; the mol ratio of the ammonia gas to the hydrogen peroxide in the step (1) is 0.3: 1;
(3) the ozone is divided into ozone I and ozone II, the absorption liquid is divided into absorption liquid I and absorption liquid II, the ozone I and the absorption liquid I are mixed and sprayed into a nitrogen oxide absorption device 8, the ozone II and the absorption liquid II are mixed and sprayed into the desulfurization and denitrification reactor, and the spraying port of the ozone I is positioned below the spraying port of the ozone II; the flow ratio of the ozone I to the ozone II is 5:1, and the flow ratio of the absorption liquid I to the absorption liquid II is 1: 2; spraying ozone and absorption liquid into a nitrogen oxide absorption device 8 together to absorb the activated gas obtained in the step (2) to obtain purified gas and absorbed liquid; the liquid-gas ratio of the absorption liquid to the activated gas is 5L/Nm3(ii) a The molar ratio of the ozone to NO in the flue gas is 0.2: 1; the absorption liquid is sodium hydroxide solution with pH value of 10.
Application of Nitrogen oxides and SO in purified gas obtained in examples 1 to 15 to flue gas Analyzer2The concentration was tested.
The removal rate of the obtained nitrogen oxides is as follows:
[ (flue gas nitrogen oxide mass concentration-purified gas nitrogen oxide mass concentration)/flue gas nitrogen oxide mass concentration ]. times.100%;
the SO obtained2The removal rate is:
[ (flue gas SO)2Mass concentration-purified gas SO2Mass concentration)/flue gas SO2Mass concentration]×100％；
The results obtained are shown in table 1.
TABLE 1
| SO2Removal Rate (%) | Removal rate of nitrogen oxide (%) | |
| Application example 1 | 99.1 | 96.8 |
| Application example 2 | 99.0 | 96.5 |
| Application example 3 | 98.5 | 96.1 |
| Application example 4 | 98.7 | 96.1 |
| Application example 5 | 98.6 | 96.3 |
| Application example 6 | 99.4 | 97.5 |
| Application example 7 | 99.2 | 97.2 |
| Application example 8 | 98.8 | 96.9 |
| Application example 9 | 98.9 | 97.0 |
| Application example 10 | 98.8 | 97.1 |
| Application example 11 | 99.5 | 98.1 |
| Application example 12 | 99.3 | 98.0 |
| Application example 13 | 99.0 | 97.7 |
| Application example 14 | 99.0 | 97.5 |
| Application example 15 | 99.9 | 97.6 |
Can know by table 1, compare the utility model discloses embodiment 6-10 can know with embodiment 1-5 for the absorption liquid that absorption liquid feeding device 1 provided carries out heat transfer with the flue gas and sets up and make flue gas and absorption liquid carry out the heat transfer with heat transfer device 2 of heat transfer, not only utilizes the waste heat of flue gas, can also make the flue gas reduce to the suitable temperature when working with hydrogen peroxide, and make the absorption liquid heat up in order to promote ozone oxidation to absorb in coordination.
It can be seen from the embodiments 11-15 and 6-10 of the present invention that the arrangement of the 2 gas-liquid mixing/injecting devices 91 improves the ozone utilization rate when the residual nitrogen oxide is oxidized by ozone, so as to further reduce the contents of the nitrogen oxide and the sulfur oxide in the finally obtained purified gas.
In summary, the system firstly utilizes the oxidant provided by the oxidant supply device to treat the sulfur oxides and the nitrogen oxides in the flue gasThe method comprises the steps of treating, namely separating sulfur oxides from nitrogen oxides, performing electron beam irradiation on excessive oxygen and water vapor by using an electron beam generating device, oxidizing the nitrogen oxides by using generated strong oxidizing free radicals, and then treating residual nitrogen oxides by matching with a small amount of ozone, wherein SO in the flue gas is finally treated2The removal rate of the nitrogen oxide can reach 99.9 percent, and the removal rate of the nitrogen oxide can reach 97.7 percent.
The applicant states that the above description is only a specific embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and those skilled in the art should understand that any changes or substitutions easily conceivable by those skilled in the art within the technical scope of the present invention are within the protection scope and the disclosure scope of the present invention.
Claims (5)
1. The system for desulfurization and denitrification by electron beam in cooperation with oxidant is characterized by comprising a gas-liquid mixing device, a oxysulfide absorbing device, a static mixer, a nitric oxide absorbing device, an oxidant supplying device, a gas-liquid mixing device, an electron beam generating device, an ammonia supplying device, an ozone generating device and at least 1 gas-liquid mixing and spraying device;
the gas-liquid mixing device, the oxysulfide absorbing device, the static mixer and the nitric oxide absorbing device are sequentially connected;
the flue gas and the oxidant provided by the oxidant supply device flow into the oxysulfide absorption device after being mixed in the gas-liquid mixing device;
the tail end of the static mixer is provided with an electron beam generating device, and gas discharged by the oxysulfide absorbing device is mixed with ammonia gas provided by the ammonia supply device in the static mixer and flows into the nitric oxide absorbing device after flowing through the electron beam generating device;
and the side wall of the nitrogen oxide absorption device is provided with a gas-liquid mixing and spraying device, and the gas-liquid mixing and spraying device is used for spraying the absorption liquid provided by the absorption liquid supply device and the ozone provided by the ozone generating device into the nitrogen oxide absorption device together by the gas-liquid mixing and spraying device.
2. The system for desulfurization and denitrification with electron beam and oxidant in coordination according to claim 1, characterized in that the system for desulfurization and denitrification with electron beam and oxidant further comprises a heat exchange device, wherein the heat exchange device is used for heat exchange between the absorption liquid provided by the absorption liquid supply device and the flue gas;
mixing the heat-exchanged flue gas with an oxidant provided by an oxidant supply device in a gas-liquid mixing device; the absorption liquid after heat exchange and ozone provided by the ozone generating device are sprayed into the nitrogen oxide absorption device by the gas-liquid mixing and spraying device.
3. The system for desulfurization and denitrification with electron beam and oxidant in cooperation according to claim 1, characterized in that the sidewall of the nitrogen oxide absorption device is provided with 1-3 gas-liquid mixing and injecting devices.
4. The system for desulfurization and denitrification with electron beam and oxidant in cooperation according to claim 3, characterized in that the sidewall of the nitrogen oxide absorption device is provided with 2 gas-liquid mixing and spraying devices.
5. The system for desulfurization and denitrification with cooperation of electron beam and oxidant according to claim 4, wherein the 2 gas-liquid mixing and injecting devices are arranged on the side wall of the desulfurization and denitrification reactor in an up-down relationship, and the discharge port of the gas-liquid mixing and injecting device at the bottom is arranged opposite to the gas inlet of the nitrogen oxide absorption device; the air inlet is used for being connected with an air outlet of the static mixer.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111495158A (en) * | 2020-05-29 | 2020-08-07 | 广东佳德环保科技有限公司 | System and method for desulfurization and denitrification by cooperation of electron beam and oxidant |
| CN115337745A (en) * | 2022-09-28 | 2022-11-15 | 联峰钢铁（张家港）有限公司 | Flue gas desulfurization and denitrification system |
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2020
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111495158A (en) * | 2020-05-29 | 2020-08-07 | 广东佳德环保科技有限公司 | System and method for desulfurization and denitrification by cooperation of electron beam and oxidant |
| CN111495158B (en) * | 2020-05-29 | 2024-02-27 | 广东佳德环保科技有限公司 | System and method for desulfurizing and denitrating by electron beam cooperated with oxidant |
| CN115337745A (en) * | 2022-09-28 | 2022-11-15 | 联峰钢铁（张家港）有限公司 | Flue gas desulfurization and denitrification system |
| CN115337745B (en) * | 2022-09-28 | 2023-09-12 | 联峰钢铁（张家港）有限公司 | Flue gas desulfurization and denitrification system |
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