CN212492355U - Ozone oxidation is SOx/NOx control system of ammonia process in coordination - Google Patents
Ozone oxidation is SOx/NOx control system of ammonia process in coordination Download PDFInfo
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- CN212492355U CN212492355U CN202020949521.2U CN202020949521U CN212492355U CN 212492355 U CN212492355 U CN 212492355U CN 202020949521 U CN202020949521 U CN 202020949521U CN 212492355 U CN212492355 U CN 212492355U
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Abstract
The utility model provides a desulfurization and denitrification system adopting an ozone oxidation and ammonia method, which comprises a first absorption device and a second absorption device which are sequentially communicated along the flow direction of flue gas; an ozone generating device is connected into an inlet flue of the first absorption device; the second absorption device is internally and sequentially divided into a circulating spraying area and at least two layers of multi-effect spraying areas from bottom to top along the flow direction of the flue gas, the circulating spraying area is externally connected with at least two absorbent storage tanks, the absorbent storage tanks are respectively and independently connected into the multi-effect spraying areas, and the absorbent storage tanks respectively supply absorbent to the circulating spraying area and the multi-effect spraying areas; the circulating spraying area is externally connected with a recovery unit. The utility model discloses a two tower structures absorb, have prolonged the dwell time of absorbent in the tower, have increased the contact time with the flue gas, have improved SOx/NOx control's efficiency. Adopts a mixed absorbent of ammonia water and calcium-based absorbent to absorb NO in the smokexAnd the fertilizer is converted into fertilizer and gypsum with higher added value.
Description
Technical Field
The utility model belongs to the technical field of SOx/NOx control, a SOx/NOx control system is related to, especially relate to a SOx/NOx control system of ozone oxidation ammonia process in coordination.
Background
In recent years, the flue gas SO of non-electric industries such as steel, coking, metallurgy and the like in China2、NOxThe emission reduction is widely concerned by people. The national and local governments are continuously coming out of increasingly strict emission standards, so that the industry faces huge emission reduction pressure. For example, in the industries of iron and steel and coking, sintering flue gas and coke oven flue gas are the main SO2And NOxA source of emissions. The emission temperature of the flue gas is generally low (150-. By raising the temperature of the flue gasAlthough matching with the traditional SCR technology can be realized, the energy consumption is huge and the cost is high. Therefore, the non-electric industries such as steel and iron, coking and the like have urgent technical requirements on low-cost desulfurization and denitrification of low-temperature flue gas.
For the removal of sulfur dioxide, a wet flue gas desulfurization technology is commonly used in engineering, the wet flue gas desulfurization technology is a gas-liquid reaction, the reaction speed is high, the desulfurization efficiency is high and is generally higher than 90%, the technology is mature, and the application range is wide. The wet desulphurization technology is mature, the production operation is safe and reliable, and the wet desulphurization technology always occupies the dominant position in a plurality of desulphurization technologies, and accounts for more than 80 percent of the total installed capacity of desulphurization. The product is liquid or sludge, which is difficult to treat, the equipment is seriously corroded, the flue gas after washing needs to be reheated, the energy consumption is high, the occupied area is large, and the investment and the operating cost are high. The system is complex, the equipment is huge, the water consumption is large, the one-time investment is high, and the method is generally suitable for large-scale power plants. The common wet flue gas desulfurization techniques include limestone-gypsum method and ammonia method.
The limestone-gypsum method is to utilize limestone or lime slurry to absorb SO in flue gas2To form calcium sulfite, separated calcium sulfite (CaSO)3) Can be discarded or oxidized to calcium sulfate (CaSO)4) Recovered as gypsum. The method is the most mature desulfurization process with the most stable operation condition in the world at present, and the desulfurization efficiency reaches more than 90 percent.
Ammonia desulphurization is one kind of wet desulphurization process, and the apparatus has ammonia or ammonium sulfite as absorbent to absorb SO in fume2And the method is widely applied to wet desulphurization processes at home and abroad. It features high desulfurizing rate, stable operation, high use value of desulfurizing by-product ammonium sulfate, and no waste water or dregs.
However, ammonia desulfurization also has some problems at present: the circulating liquid contains the para-SO2The ammonium sulfite has absorption effect and also contains a large amount of ammonium sulfate components, so that a large amount of energy consumption and waste of power of the circulating liquid pump are caused; the consumption of the ammonia absorbent is large and the problem of ammonia escape exists; the smoke at the outlet is easy to carry small liquid drops and aerosol, and is difficult to completely remove; by-product sulfuric acidThe quality of the ammonium is not high, and the investment and the operation cost of the total equipment and devices are high. Therefore, the structure of the ammonia desulfurization and denitrification device still has a larger improvement space, and the efficient, stable and low-cost wet desulfurization and denitrification device is researched and developed, so that the ammonia desulfurization and denitrification device has strong practical significance and popularization value.
However, both of these systems are difficult to treat nitrogen oxides, and have serious phenomena of alkaline liquid drops in the outlet flue gas, which causes secondary pollution to the environment. For removing nitrogen oxides, the traditional method mainly adopts a selective catalytic reduction method and a selective non-catalytic reduction method, wherein the former has the problems of easy poisoning of a catalyst, ammonia leakage and the like although the efficiency is higher, and the latter has the problems of low efficiency, higher applicable temperature and narrow temperature window range.
CN206008418U discloses a high-efficiency energy-saving gas-liquid coupling oxidation desulfurization and denitrification device, which comprises an absorption tower, wherein the lower part of the absorption tower is provided with a flue gas inlet, the absorption tower is internally provided with a demisting section, an absorption section, an oxidation section and a concentration section, the demisting section comprises a first-stage demister arranged at the upper part of the absorption tower, a washing layer is arranged below the first-stage demister, the absorption section comprises an absorption layer positioned below the washing layer, the concentration section comprises a concentration spraying layer arranged above the flue gas inlet and a concentration tank positioned at the bottom of the absorption tower, the oxidation section comprises an oxidation tank internally communicated with ozone, the oxidation tank is arranged between the absorption layer and the concentration spraying layer and is connected with the concentration spraying layer, a hydrogen peroxide solution inlet pipe is arranged above the oxidation tank on the oxidation section of the desulfurization tower, the demisting section comprises an absorption tank communicated with the top of the absorption tower, the absorption tank is arranged at one side of the absorption, a second-stage demister is arranged in the flue gas outlet.
CN101053747 discloses a wet ammonia flue gas cleaning process for simultaneous desulfurization and denitrification, which comprises the following steps of pre-dedusting the flue gas to be desulfurized: 1) hydrogen peroxide or ozone is used as an oxidant, air is used as an atomizing medium, and the oxidant and the atomizing medium are uniformly sprayed into the flue gas subjected to pre-dedusting treatment, so that nitrogen monoxide in the flue gas not only chemically reacts with the hydrogen peroxide or ozone, but also chemically reacts with oxygen in the air, and nitrogen dioxide gas is generated; 2) ammonia water is used as a desulfurization and denitrification agent and is sprayed into the flue gas after peroxidation treatment, so that sulfur dioxide and nitrogen dioxide in the flue gas respectively and chemically react with the ammonia water to generate a mixture of ammonium sulfite, ammonium nitrate and ammonium nitrite; 3) air is used as an oxidant and is sprayed into a mixture of ammonium sulfite, ammonium nitrate and ammonium nitrite generated by desulfurization and denitrification reaction, so that the ammonium sulfite and ammonium nitrite in the mixture and oxygen in the air generate sufficient oxidation reaction to generate byproducts of ammonium sulfate and ammonium nitrate; 4) and demisting the flue gas subjected to desulfurization and denitrification reaction, and removing liquid drops carried in the flue gas to obtain the clean flue gas subjected to desulfurization and denitrification simultaneously.
CN101934191B discloses a method for simultaneously desulfurizing and denitrating flue gas by an ammonia process, which is carried out in a desulfurization and denitrification system, wherein the desulfurization and denitrification system comprises a desulfurization and denitrification tower, the flue gas conveyed by a draught fan enters an absorption section from a flue gas inlet in the middle of the desulfurization and denitrification tower, contacts with absorption liquid from a denitrification spraying layer and a desulfurization spraying layer, denitrates and desulfurizes, meanwhile, the flue gas is cooled to below 70 ℃, and upwards enters an upper washing demisting section, and the unreacted ammonia in the flue gas is absorbed and removed through the washing layer and the water spraying layer, and then the pure flue gas is discharged from a flue gas outlet after being demisted through the demisting layer; the upper part of the oxidation section at the lower part of the desulfurization and denitrification tower is a denitrification circulation layer, the middle part of the oxidation section is a desulfurization circulation layer, the bottom of the oxidation section is an oxidation layer, and the oxidation layer is provided with an air distributor; denitration circulating layer sprays the layer through the outer circulation pipeline of tower and communicates with each other with the lower floor denitration of absorption section, the desulfurization circulating layer sprays the layer through the outer circulation pipeline of tower and the middle-level desulfurization of absorption section and communicates with each other, the oxide layer sprays the layer through the outer circulation pipeline of tower and the desulfurization of the upper strata of absorption section and communicates with each other, each circulating line is equipped with the circulating pump respectively, the oxide layer bottom is passed through the bleeder pump and is communicated with ammonium sulfate recovery unit, ammonium sulfate recovery unit includes the circulation groove of connecting gradually, the swirler, centrifuge, the desiccator, simultaneously, the last overflow mouth of swirler and centrifuge's liquid outlet are connected to the circulation groove.
When sulfur dioxide and nitric oxide exist in flue gas at the same time, a series of problems of mutual influence of two processes, high energy consumption and operation cost, large occupied area, high equipment investment and the like exist for respectively treating the sulfur dioxide and the nitric oxide.
SUMMERY OF THE UTILITY MODEL
Not enough to prior art exist, the utility model aims to provide a SOx/NOx control system of ozone oxidation ammonia process in coordination, the utility model discloses a two tower structures absorb, have prolonged the dwell time of absorbent in the tower, have increased the contact time with the flue gas, have improved SOx/NOx control's efficiency. Meanwhile, the NO in the smoke is absorbed by adopting a mixed absorbent of ammonia water and a calcium-based absorbentxAnd the fertilizer is converted into fertilizer and gypsum with higher added value.
To achieve the purpose, the utility model adopts the following technical proposal:
in a first aspect, the utility model provides a SOx/NOx control system of ozone oxidation ammonia process in coordination, SOx/NOx control system include along the first absorbing device and the second absorbing device that the flue gas flow direction communicates in proper order.
And an ozone generating device is connected into an inlet flue of the first absorption device.
The second absorption device is internally and sequentially divided into a circulating spraying area and at least two layers of multi-effect spraying areas from bottom to top along the flow direction of flue gas, the circulating spraying area is externally connected with at least two absorbent storage tanks, the absorbent storage tanks are respectively and independently connected into the multi-effect spraying areas, and the absorbent storage tanks respectively supply absorbent to the circulating spraying area and the multi-effect spraying areas.
The recycling spraying area is externally connected with a recycling unit, and the recycling unit is used for recycling the ineffective absorbent generated after spraying.
The utility model discloses a two tower structures absorb, create the absorption condition of high gas velocity and high pH in the first absorbing device, the absorbent upwards sprays and forms the adverse current with the interior flue gas of tower, and the absorbent falls back under the action of gravity, forms the following current with the flue gas at the in-process that falls back, has prolonged the dwell time of absorbent in the tower, has increased the contact time with the flue gas, has improved SOx/NOx control's efficiency. Meanwhile, the flue gas temperature is reduced and the flue gas amount is reduced through the spraying and cooling of the first absorption device, and after the flue gas enters the second absorption device, the liquid-gas ratio is increased under the condition of the same spraying amount, so that the desulfurization and denitrification efficiency is further improved. The second absorption device is internally provided with the absorption conditions of low gas velocity and low pH value, the oxidation efficiency is enhanced, meanwhile, the excessive ammonia in the first absorption device can be fully reacted to generate ammonium sulfate and ammonium nitrate, and the excessive calcium-based absorbent can be fully reacted to obtain the calcium sulfite.
As an optimized technical proposal, the ozone generating device is connected into the inlet flue through the ozone conveying pipeline.
The outlet end of the ozone conveying pipeline extends into the inlet flue.
The outlet end of the ozone conveying pipeline is provided with a distribution feeding device.
The spraying direction of the distribution feeding device is opposite to the flow direction of the flue gas, and the flue gas is in countercurrent contact with the ozone after being introduced into the inlet flue.
Along the flue gas flow direction, the inlet flue at the rear end of the ozone generating device is internally provided with a mixing device, and the flue gas is mixed and fully oxidized by the mixing device after contacting with the ozone.
As an optimal technical scheme, the exit end of inlet flue connect the top flue gas entry of first absorbing device, the flue gas gets into by first absorbing device top after being discharged by inlet flue.
The bottom of the first absorption device is a liquid storage tank, at least two groups of spraying devices are arranged above the liquid storage tank side by side, and the absorbent sprayed by the spraying devices falls into the bottom of the first absorption device to form the liquid storage tank.
The spraying device comprises a spraying pipeline and nozzles uniformly distributed on the spraying pipeline, and the spraying direction of the nozzles is opposite to the flow direction of the flue gas.
And the bottom of the first absorption device is externally connected with a liquid discharge pipeline.
As an optimized technical scheme, the second absorbing device inside divide into circulation along the flue gas flow direction from bottom to top in proper order and spray district, first multiple-effect and spray the district and the second multiple-effect sprays the district.
The utility model discloses divide into the two-stage multiple-effect with the second absorbing device and spray, two-layer spray space mutually independent, adopt different absorbent circulation respectively to spray, nitrogen sulphur in the progressively desorption flue gas realizes synchronous SOx/NOx control for the solution concentration who carries in the flue gas is very low, has not only alleviated the white smoke phenomenon of wet flue gas SOx/NOx control system, has also further reduced the equipment corrosion, and desulfurization efficiency and denitration efficiency can reach more than 95%, and the liquid drop clearance reaches more than 70%.
As an optimal technical scheme, the circulation spray zone including the circulation spray pond and be located the circulation spray set of circulation spray pond top, the absorbent that the circulation spray set sprayed form after falling into second absorbing device bottom circulation spray pond.
The circulating spray tank is connected with a circulating spray device through an external circulating spray pipeline.
The first absorption device is communicated with the second absorption device through a flue, flue gas flows into the second absorption device through the flue after being discharged by the first absorption device, the inlet end of the flue is positioned between the liquid storage tank of the first absorption device and the spray device, and the outlet end of the flue is positioned between the circulating spray tank of the second absorption device and the circulating spray device.
The circulating spray tank is respectively and independently connected with the first absorbent storage tank and the second absorbent storage tank, and is also externally connected with a spray device of the first absorbent device.
And the liquid storage tank of the first absorption device is connected with the circulating spray tank of the second absorption device, and the liquid storage tank and the circulating spray tank are connected to realize liquid level balance.
As a preferred technical scheme of the utility model, first absorbent storage tank in store and have calcium-based absorbent, second absorbent storage tank in store and have aqueous ammonia.
The first absorbent storage tank and the second absorbent storage tank respectively provide a calcium-based absorbent and ammonia water for the circulating spray pond.
Ammonia water with the concentration of 20-30 wt% is used as an absorbent for desulfurization and denitrification and is respectively mixed with the ammonia water in the flue gasSO2And NO2The reaction takes place to produce ammonium sulfate and ammonium nitrate. The main chemical reactions are as follows:
2NH3+SO2+H2O＝(NH4)2SO3
(NH4)2SO3+1/2O2＝(NH4)2SO4
NH3+NO2+H2O＝NH4NO3
as an optimized technical proposal of the utility model, the calcium-based absorbent is any one of quicklime, limestone, steel slag, papermaking white mud or carbide slag.
As a preferred technical solution of the present invention, the first multi-effect spraying area comprises a first spraying device and a first spraying device located above the first spraying device.
The first absorbent storage tank is respectively and independently connected with the first injection device and the first spraying device, the first absorbent storage tank respectively provides a calcium-based absorbent for the first injection device and the first spraying device, a desulfurization and denitrification space is formed between the first injection device and the first spraying device, and flue gas is contacted with the calcium-based absorbent in the desulfurization and denitrification space.
The spraying direction of the first spraying device is opposite to the spraying direction of the first spraying device.
The second multi-effect spraying area comprises a second spraying device and a second spraying device positioned above the second spraying device.
As an optimal technical scheme, the second absorbent storage tank insert second injection apparatus and second spray set respectively independently, the second absorbent storage tank provide the aqueous ammonia to second injection apparatus and second spray set respectively, second injection apparatus and second spray set between form SOx/NOx control space, the flue gas contacts with the aqueous ammonia in SOx/NOx control space.
The spraying direction of the second spraying device is opposite to the spraying direction of the second spraying device.
And a demisting device is also arranged at the smoke outlet of the second absorption device.
As an optimal technical scheme, the recovery unit include cyclone, centrifugal separation device, drying device, oxidation groove and filter equipment, circulation spray tank bottom arrange the flow direction along the absorbent outside and connect gradually cyclone and centrifugal separation device, centrifugal separation device's discharge gate connect drying device, centrifugal separation device's liquid outlet dock the oxidation groove, oxidation groove and filter equipment circulation connection.
Preferably, the oxidation tank is externally connected with a blower.
The utility model provides a SOx/NOx control system of ozone oxidation ammonia process in coordination's theory of operation does:
the method comprises the following steps of (I) carrying out countercurrent contact, mixing by a mixing device, fully oxidizing, and then sending into a first absorption device; the first absorbent storage tank and the second absorbent storage tank respectively inject calcium-based absorbent and ammonia water into a circulating spray tank of the second absorption device, mixed absorbent formed in the circulating spray tank is introduced into the spray device of the first absorption device, and oxidized flue gas is introduced from the top of the first absorption device and is in countercurrent contact with the mixed absorbent sprayed by the spray device;
(II) the flue gas is discharged from the first absorption device and enters a circulating spraying area of a second absorption device through a flue, and a mixed absorbent formed in the circulating spraying pool is circularly sprayed in the circulating spraying area and is in countercurrent contact with the flue gas; the flue gas continuously rises to enter a first multi-effect spraying area, the calcium-based absorbent stored in a first desulfurizer storage tank is respectively introduced into a first injection device and a first spraying device, the first injection device and a second spraying device spray the calcium-based absorbent oppositely, and the flue gas is fully contacted with the calcium-based absorbent; the flue gas continuously rises to enter a second multi-effect spraying area, ammonia water stored in a second desulfurizer storage tank is respectively introduced into a second injection device and a second spraying device, the second injection device and the second spraying device spray the ammonia water oppositely, the flue gas is fully contacted with the ammonia water, and the flue gas after deep desulfurization and denitrification is demisted and then is discharged from the top of a second absorption device;
(III) continuously forming an ineffective absorbent containing ammonium sulfate, ammonium nitrate and calcium sulfite in the circulating spray tank along with the spraying process in the second absorption device, discharging the ineffective absorbent when the solid content in the ineffective absorbent reaches 15-20%, and separating the mixed absorbent collected in the circulating spray tank by a cyclone separation device and a centrifugal separation device in sequence to obtain slurry and clear liquid; wherein, the clear liquid enters a drying device for drying and dehydration to form ammonium sulfate and ammonium nitrate crystals; the slurry falls into an oxidation tank to be in contact oxidation with air introduced by a blower, calcium sulfite in the slurry is converted into calcium sulfate, the oxidized slurry is filtered to obtain gypsum, and the filtrate is returned to the oxidation tank for recycling.
The system refers to an equipment system, or a production equipment.
Compared with the prior art, the beneficial effects of the utility model are that:
(1) the utility model discloses a two tower structures absorb, create the absorption condition of high gas velocity and high pH in the first absorbing device, the absorbent upwards sprays and forms the adverse current with the interior flue gas of tower, and the absorbent falls back under the action of gravity, forms the following current with the flue gas at the in-process that falls back, has prolonged the dwell time of absorbent in the tower, has increased the contact time with the flue gas, has improved SOx/NOx control's efficiency. Meanwhile, the flue gas temperature is reduced and the flue gas amount is reduced through the spraying and cooling of the first absorption device, and after the flue gas enters the second absorption device, the liquid-gas ratio is increased under the condition of the same spraying amount, so that the desulfurization and denitrification efficiency is further improved. The second absorption device is internally provided with the absorption conditions of low gas velocity and low pH value, the oxidation efficiency is enhanced, meanwhile, the excessive ammonia in the first absorption device can be fully reacted to generate ammonium sulfate and ammonium nitrate, and the excessive calcium-based absorbent can be fully reacted to obtain the calcium sulfite.
(2) The utility model discloses divide into the two-stage multiple-effect with the second absorbing device and spray, two-layer spray space mutually independent, adopt different absorbent circulation respectively to spray, the nitrogen sulphur in the progressively desorption flue gas realizes synchronous SOx/NOx control for the solution concentration who carries in the flue gas is very low, has not only alleviated the white smoke phenomenon of wet flue gas SOx/NOx control system, has also further reduced the equipment corrosion, and desulfurization efficiency and denitration efficiency can reach more than 95%.
(3) The utility model provides a SOx/NOx control device improves denitration rate by a wide margin to with the NO in the flue gasxAnd the fertilizer is converted into fertilizer and gypsum with higher added value.
Drawings
Fig. 1 is a schematic structural diagram of a desulfurization and denitrification system provided by an embodiment of the present invention.
Wherein, 1-inlet flue; 2-an ozone generating device; 3-a mixing device; 4-a first absorption device; 5-a liquid storage tank; 6-a spraying device; 7-a second absorption device; 8-circulating spraying area; 9-a first multi-effect spraying area; 10-a second multi-effect spraying area; 11-circulating spray pond; 12-a circulating spray device; 13-a first injection device; 14-a first spray device; 15-a second spraying device; 16-a second spraying device; 17-a demisting device; 18-a first absorbent storage tank; 19-a second absorbent storage tank; 20-a cyclonic separation device; 21-a centrifugal separation device; 22-a drying device; 23-an oxidation tank; 24-a filtration device; 25-a fan.
Detailed Description
It is to be understood that in the description of the present invention, the terms "central," "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in the orientation or positional relationship indicated in the drawings for the purpose of convenience and simplicity of description, and are not intended to indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are not to be construed as limiting the present invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
It should be noted that, unless explicitly stated or limited otherwise, the terms "disposed," "connected" and "connected" in the description of the present invention are to be construed broadly, and may for example be fixedly connected, detachably connected or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
The technical solution of the present invention is further explained by the following embodiments with reference to the accompanying drawings.
In one embodiment, the desulfurization and denitrification system with ozone oxidation and ammonia process, as shown in fig. 1, comprises a first absorption device 4 and a second absorption device 7 which are communicated in sequence along the flow direction of flue gas. An ozone generating device 2 is connected into an inlet flue 1 of the first absorption device 4. The second absorption device 7 is internally sequentially divided into a circulating spraying area 8 and at least two layers of multi-effect spraying areas from bottom to top along the flow direction of flue gas, the circulating spraying area 8 is externally connected with at least two absorbent storage tanks, the absorbent storage tanks are respectively and independently connected into the multi-effect spraying areas, and the absorbent storage tanks respectively supply absorbent to the circulating spraying area 8 and the multi-effect spraying areas. The circulating spraying area 8 is externally connected with a recovery unit, and the recovery unit is used for recovering and utilizing the ineffective absorbent generated after spraying.
Ozone generating device 2 inserts inlet flue 1 through ozone conveying line, and inside ozone conveying line's exit end stretched into inlet flue 1, ozone conveying line's exit end was provided with the distribution and throws the feeder apparatus, and the spraying direction that the feeder apparatus was thrown in the distribution is opposite with the flue gas flow direction, and the flue gas contacts with ozone against the current after letting in inlet flue 1. Along the flue gas flow direction, be provided with mixing arrangement 3 in the import flue 1 of ozone generating device 2 rear end, the flue gas is contacted with ozone after through mixing arrangement 3 intensive oxidation.
The outlet end of the inlet flue 1 is connected with the top flue gas inlet of the first absorption device 4, and flue gas is discharged from the inlet flue 1 and then enters from the top of the first absorption device 4. The bottom of the first absorption device 4 is a liquid storage tank 5, at least two groups of spraying devices 6 are arranged above the liquid storage tank 5 side by side, and the absorbent sprayed by the spraying devices 6 falls into the bottom of the first absorption device 4 to form the liquid storage tank 5. The spraying device 6 comprises a spraying pipeline and nozzles uniformly distributed on the spraying pipeline, and the spraying direction of the nozzles is opposite to the flow direction of the flue gas. External drainage pipeline at bottom of first absorption device 4
The interior of the second absorption device 7 is sequentially divided into a circulating spraying area 8, a first multi-effect spraying area 9 and a second multi-effect spraying area 10 from bottom to top along the flow direction of the flue gas.
The circulating spraying area 8 comprises a circulating spraying pool 11 and a circulating spraying device 12 positioned above the circulating spraying pool 11, the absorbent sprayed by the circulating spraying device 12 falls into the bottom of the second absorption device 7 to form the circulating spraying pool 11, and the circulating spraying pool 11 is connected with the circulating spraying device 12 through an external circulating spraying pipeline.
The first absorption device 4 is communicated with the second absorption device 7 through a flue, flue gas is discharged by the first absorption device 4 and then flows into the second absorption device 7 through the flue, the inlet end of the flue is positioned between the liquid storage tank 5 of the first absorption device 4 and the spraying device 6, and the outlet end of the flue is positioned between the circulating spraying tank 11 of the second absorption device 7 and the circulating spraying device 12.
The circulating spray tank 11 is respectively and independently connected with a first absorbent storage tank 18 and a second absorbent storage tank 19, and the circulating spray tank 11 is also externally connected with a spray device 6 of the first absorption device 4. The first absorbent storage tank 18 stores a calcium-based absorbent, the calcium-based absorbent comprises one or a combination of at least two of quick lime, limestone, steel slag, papermaking white mud and carbide slag, and the second absorbent storage tank 19 stores ammonia water. The first absorbent storage tank 18 and the second absorbent storage tank 19 respectively supply the calcium-based absorbent and the ammonia water to the circulating spray tank 11. The liquid storage tank 5 of the first absorption device 4 is connected with the circulating spray tank 11 of the second absorption device 7, and the liquid level balance between the liquid storage tank 5 and the circulating spray tank 11 is realized through the connection of the liquid storage tank 5 and the circulating spray tank.
The first multi-effect spraying area 9 comprises a first spraying device 13 and a first spraying device 14 positioned above the first spraying device 13; the first absorbent storage tank 18 is respectively and independently connected to the first injection device 13 and the first spraying device 14, the first absorbent storage tank 18 respectively provides calcium-based absorbent for the first injection device 13 and the first spraying device 14, a desulfurization and denitrification space is formed between the first injection device 13 and the first spraying device 14, flue gas is contacted with the calcium-based absorbent in the desulfurization and denitrification space, and the injection direction of the first injection device 13 is opposite to the spraying direction of the first spraying device 14.
The second multi-effect spraying area 10 comprises a second spraying device 15 and a second spraying device 16 located above the second spraying device 15, a second absorbent storage tank 19 is respectively and independently connected to the second spraying device 15 and the second spraying device 16, the second absorbent storage tank 19 respectively provides ammonia water for the second spraying device 15 and the second spraying device 16, a desulfurization and denitrification space is formed between the second spraying device 15 and the second spraying device 16, and flue gas is contacted with the ammonia water in the desulfurization and denitrification space. The spraying direction of the second spraying device 15 is opposite to the spraying direction of the second spraying device 16. The flue gas outlet of the second absorption device 7 is also provided with a demisting device 17.
The recycling unit comprises a cyclone separation device 20, a centrifugal separation device 21, a drying device 22, an oxidation tank 23 and a filtering device 24, the bottom of the circulating spray pond 11 is sequentially connected with the cyclone separation device 20 and the centrifugal separation device 21 along the outward discharge direction of the absorbent, the discharge port of the centrifugal separation device 21 is connected with the drying device 22, the liquid outlet of the centrifugal separation device 21 is in butt joint with the oxidation tank 23, the oxidation tank 23 is in circulating connection with the filtering device 24, and the oxidation tank 23 is further externally connected with an air blower 25.
Example 1
The embodiment provides a desulfurization and denitrification method by using ozone oxidation in cooperation with an ammonia method, which specifically comprises the following steps:
(1) the ozone generating device 2 introduces ozone into the inlet flue 1, the flue gas is in countercurrent contact with the ozone after being introduced into the inlet flue 1, the molar ratio of the ozone introduced into the inlet flue 1 to NO in the flue gas is 0.8, and the flue gas is mixed, fully oxidized and then sent into the first absorbing device 4 through the mixing device 3; the first absorbent storage tank 18 and the second absorbent storage tank 19 respectively inject quick lime and ammonia water into the circulating spray tank 11 of the second absorption device 7, a mixed absorbent formed in the circulating spray tank 11 is introduced into the spray device 6 of the first absorption device 4, the pH value of the mixed absorbent sprayed in the first absorption device 4 is controlled to be 5.3, oxidized flue gas is introduced from the top of the first absorption device 4, the flow rate of the flue gas is controlled to be 4.5m/s, and the flue gas is in countercurrent contact with the mixed absorbent sprayed by the spray device 6;
(2) the flue gas is discharged from the first absorption device 4 and enters a circulating spray area 8 of a second absorption device 7 through a flue, the pH value of a mixed absorbent circularly sprayed in the second absorption device 7 is controlled to be 4.5, the flow rate of the flue gas in the second absorption device 7 is controlled to be 3.5m/s, the mixed absorbent formed in a circulating spray pool 11 is circularly sprayed in the circulating spray area 8 and is in countercurrent contact with the flue gas, and the liquid-gas ratio of the mixed absorbent to the flue gas is 8: 1; the flue gas continuously rises to enter a first multi-effect spraying area 9, quicklime stored in a first desulfurizer storage tank is respectively introduced into a first injection device 13 and a first spraying device 14, the first injection device 13 and a second spraying device 16 spray the quicklime oppositely, the flue gas is fully contacted with the quicklime, and the liquid-gas ratio of the quicklime to the flue gas is 5: 1; the flue gas continuously rises to enter a second multi-effect spraying area 10, ammonia water stored in a second desulfurizer storage tank is respectively introduced into a second injection device 15 and a second spraying device 16, the second injection device 15 and the second spraying device 16 spray the ammonia water oppositely, the flue gas is fully contacted with the ammonia water, and the liquid-gas ratio of the ammonia water to the flue gas is 3: 1; demisting the flue gas subjected to deep desulfurization and denitrification, and then discharging the demisted flue gas from the top of the second absorption device 7;
(3) with the proceeding of the spraying process in the second absorption device 7, the ineffective absorbent containing ammonium sulfate, ammonium nitrate and calcium sulfite is continuously formed in the circulating spraying pool 11, and when the solid content in the ineffective absorbent reaches 15%, the ineffective absorbent is discharged outside, and is sequentially separated by the cyclone separation device 20 and the centrifugal separation device 21 to obtain slurry and clear liquid; wherein, the clear liquid enters a drying device 22 for drying and dehydration to form ammonium sulfate and ammonium nitrate crystals; the slurry falls into an oxidation tank 23 to be in contact with air introduced by a blower 25 for oxidation, calcium sulfite in the slurry is converted into calcium sulfate, the oxidized slurry is filtered to obtain gypsum, and the filtrate returns to the oxidation tank 23 for recycling.
The purified flue gas discharged from the top of the second absorption device 7 was subjected to sampling test, and the desulfurization rate was calculated to be 94.6%, and the denitrification rate was calculated to be 91.2%.
Example 2
The embodiment provides a desulfurization and denitrification method by using ozone oxidation in cooperation with an ammonia method, which specifically comprises the following steps:
(1) the ozone generating device 2 introduces ozone into the inlet flue 1, the flue gas is in countercurrent contact with the ozone after being introduced into the inlet flue 1, the molar ratio of the ozone introduced into the inlet flue 1 to NO in the flue gas is 0.9, and the flue gas is mixed, fully oxidized and then sent into the first absorbing device 4 through the mixing device 3; limestone and ammonia water are respectively injected into a circulating spray tank 11 of a second absorption device 7 from a first absorbent storage tank 18 and a second absorbent storage tank 19, a mixed absorbent formed in the circulating spray tank 11 is introduced into a spray device 6 of the first absorption device 4, the pH value of the mixed absorbent sprayed in the first absorption device 4 is controlled to be 5.6, oxidized flue gas is introduced from the top of the first absorption device 4, the flow rate of the flue gas is controlled to be 4.2m/s, and the flue gas is in countercurrent contact with the mixed absorbent sprayed by the spray device 6;
(2) the flue gas is discharged from the first absorption device 4 and enters a circulating spray area 8 of a second absorption device 7 through a flue, the pH value of a mixed absorbent circularly sprayed in the second absorption device 7 is controlled to be 4.7, the flow rate of the flue gas in the second absorption device 7 is controlled to be 3.4m/s, the mixed absorbent formed in a circulating spray pool 11 is circularly sprayed in the circulating spray area 8 and is in countercurrent contact with the flue gas, and the liquid-gas ratio of the mixed absorbent to the flue gas is 8.5: 1; the flue gas continuously rises to enter a first multi-effect spraying area 9, limestone stored in a first desulfurizer storage tank is respectively introduced into a first injection device 13 and a first spraying device 14, the limestone is oppositely sprayed by the first injection device 13 and a second spraying device 16, the flue gas is fully contacted with the limestone, and the liquid-gas ratio of the limestone to the flue gas is 6: 1; the flue gas continuously rises to enter a second multi-effect spraying area 10, ammonia water stored in a second desulfurizer storage tank is respectively introduced into a second injection device 15 and a second spraying device 16, the second injection device 15 and the second spraying device 16 spray the ammonia water oppositely, the flue gas is fully contacted with the ammonia water, and the liquid-gas ratio of the ammonia water to the flue gas is 3.5: 1; demisting the flue gas subjected to deep desulfurization and denitrification, and then discharging the demisted flue gas from the top of the second absorption device 7;
(3) with the proceeding of the spraying process in the second absorption device 7, the ineffective absorbent containing ammonium sulfate, ammonium nitrate and calcium sulfite is continuously formed in the circulating spraying pool 11, and when the solid content in the ineffective absorbent reaches 16%, the ineffective absorbent is discharged outside, and is sequentially separated by the cyclone separation device 20 and the centrifugal separation device 21 to obtain slurry and clear liquid; wherein, the clear liquid enters a drying device 22 for drying and dehydration to form ammonium sulfate and ammonium nitrate crystals; the slurry falls into an oxidation tank 23 to be in contact with air introduced by a blower 25 for oxidation, calcium sulfite in the slurry is converted into calcium sulfate, the oxidized slurry is filtered to obtain gypsum, and the filtrate returns to the oxidation tank 23 for recycling.
The purified flue gas discharged from the top of the second absorption device 7 was subjected to sampling detection, and the desulfurization rate was calculated to be 95.3%, and the denitrification rate was calculated to be 92.7%.
Example 3
The embodiment provides a desulfurization and denitrification method by using ozone oxidation in cooperation with an ammonia method, which specifically comprises the following steps:
(1) the ozone generating device 2 introduces ozone into the inlet flue 1, the flue gas is in countercurrent contact with the ozone after being introduced into the inlet flue 1, the molar ratio of the ozone introduced into the inlet flue 1 to NO in the flue gas is 1, and the flue gas is mixed by the mixing device 3, fully oxidized and then sent into the first absorbing device 4; respectively injecting steel slag and ammonia water into a circulating spray tank 11 of a second absorption device 7 by a first absorbent storage tank 18 and a second absorbent storage tank 19, introducing a mixed absorbent formed in the circulating spray tank 11 into a spray device 6 of the first absorption device 4, controlling the pH value of the mixed absorbent sprayed in the first absorption device 4 to be 6, introducing oxidized flue gas from the top of the first absorption device 4, controlling the flow velocity of the flue gas to be 4m/s, and enabling the flue gas to be in countercurrent contact with the mixed absorbent sprayed by the spray device 6;
(2) the flue gas is discharged from the first absorption device 4 and enters a circulating spray area 8 of a second absorption device 7 through a flue, the pH value of a mixed absorbent circularly sprayed in the second absorption device 7 is controlled to be 5, the flow rate of the flue gas in the second absorption device 7 is controlled to be 3.3m/s, the mixed absorbent formed in a circulating spray pool 11 is circularly sprayed in the circulating spray area 8 and is in countercurrent contact with the flue gas, and the liquid-gas ratio of the mixed absorbent to the flue gas is 9: 1; the flue gas continuously rises to enter a first multi-effect spraying area 9, steel slag stored in a first desulfurizer storage tank is respectively introduced into a first spraying device 13 and a first spraying device 14, the first spraying device 13 and a second spraying device 16 spray the steel slag oppositely, the flue gas is fully contacted with the steel slag, and the liquid-gas ratio of the steel slag to the flue gas is 7: 1; the flue gas continuously rises to enter a second multi-effect spraying area 10, ammonia water stored in a second desulfurizer storage tank is respectively introduced into a second injection device 15 and a second spraying device 16, the second injection device 15 and the second spraying device 16 spray the ammonia water oppositely, the flue gas is fully contacted with the ammonia water, and the liquid-gas ratio of the ammonia water to the flue gas is 4: 1; demisting the flue gas subjected to deep desulfurization and denitrification, and then discharging the demisted flue gas from the top of the second absorption device 7;
(3) with the proceeding of the spraying process in the second absorption device 7, the ineffective absorbent containing ammonium sulfate, ammonium nitrate and calcium sulfite is continuously formed in the circulating spraying pool 11, and when the solid content in the ineffective absorbent reaches 17%, the ineffective absorbent is discharged outside, and is sequentially separated by the cyclone separation device 20 and the centrifugal separation device 21 to obtain slurry and clear liquid; wherein, the clear liquid enters a drying device 22 for drying and dehydration to form ammonium sulfate and ammonium nitrate crystals; the slurry falls into an oxidation tank 23 to be in contact with air introduced by a blower 25 for oxidation, calcium sulfite in the slurry is converted into calcium sulfate, the oxidized slurry is filtered to obtain gypsum, and the filtrate returns to the oxidation tank 23 for recycling.
Sampling detection is carried out on the purified flue gas discharged from the top of the second absorption device 7, and the calculated desulfurization rate is 96.8%, and the denitration rate is 93.5%.
Example 4
The embodiment provides a desulfurization and denitrification method by using ozone oxidation in cooperation with an ammonia method, which specifically comprises the following steps:
(1) the ozone generating device 2 introduces ozone into the inlet flue 1, the flue gas is in countercurrent contact with the ozone after being introduced into the inlet flue 1, the molar ratio of the ozone introduced into the inlet flue 1 to NO in the flue gas is 1.1, and the flue gas is mixed, fully oxidized and then sent into the first absorbing device 4 through the mixing device 3; a first absorbent storage tank 18 and a second absorbent storage tank 19 respectively inject papermaking white mud and ammonia water into a circulating spray tank 11 of a second absorption device 7, a mixed absorbent formed in the circulating spray tank 11 is introduced into a spray device 6 of the first absorption device 4, the pH value of the mixed absorbent sprayed in the first absorption device 4 is controlled to be 6.3, oxidized flue gas is introduced from the top of the first absorption device 4, the flow rate of the flue gas is controlled to be 3.7m/s, and the flue gas is in countercurrent contact with the mixed absorbent sprayed by the spray device 6;
(2) the flue gas is discharged from the first absorption device 4 and enters a circulating spray area 8 of a second absorption device 7 through a flue, the pH value of a mixed absorbent circularly sprayed in the second absorption device 7 is controlled to be 5.2, the flow rate of the flue gas in the second absorption device 7 is controlled to be 3.2m/s, the mixed absorbent formed in a circulating spray pool 11 is circularly sprayed in the circulating spray area 8 and is in countercurrent contact with the flue gas, and the liquid-gas ratio of the mixed absorbent to the flue gas is 9.5: 1; the smoke continuously rises to enter a first multi-effect spraying area 9, the papermaking white mud stored in a first desulfurizer storage tank is respectively introduced into a first injection device 13 and a first spraying device 14, the first injection device 13 and a second spraying device 16 spray the papermaking white mud oppositely, the smoke is fully contacted with the papermaking white mud, and the liquid-gas ratio of the papermaking white mud to the smoke is 7.5: 1; the flue gas continuously rises to enter a second multi-effect spraying area 10, ammonia water stored in a second desulfurizer storage tank is respectively introduced into a second injection device 15 and a second spraying device 16, the second injection device 15 and the second spraying device 16 spray the ammonia water oppositely, the flue gas is fully contacted with the ammonia water, and the liquid-gas ratio of the ammonia water to the flue gas is 4.5: 1; demisting the flue gas subjected to deep desulfurization and denitrification, and then discharging the demisted flue gas from the top of the second absorption device 7;
(3) with the proceeding of the spraying process in the second absorption device 7, the ineffective absorbent containing ammonium sulfate, ammonium nitrate and calcium sulfite is continuously formed in the circulating spraying pool 11, and when the solid content in the ineffective absorbent reaches 18 percent, the ineffective absorbent is discharged outside, and is sequentially separated by the cyclone separation device 20 and the centrifugal separation device 21 to obtain slurry and clear liquid; wherein, the clear liquid enters a drying device 22 for drying and dehydration to form ammonium sulfate and ammonium nitrate crystals; the slurry falls into an oxidation tank 23 to be in contact with air introduced by a blower 25 for oxidation, calcium sulfite in the slurry is converted into calcium sulfate, the oxidized slurry is filtered to obtain gypsum, and the filtrate returns to the oxidation tank 23 for recycling.
The purified flue gas discharged from the top of the second absorption device 7 was subjected to sampling test, and the desulfurization rate was calculated to be 95.6%, and the denitrification rate was calculated to be 94.2%.
Example 5
The embodiment provides a desulfurization and denitrification method by using ozone oxidation in cooperation with an ammonia method, which specifically comprises the following steps:
(1) the ozone generating device 2 introduces ozone into the inlet flue 1, the flue gas is in countercurrent contact with the ozone after being introduced into the inlet flue 1, the molar ratio of the ozone introduced into the inlet flue 1 to NO in the flue gas is 1.2, and the flue gas is mixed, fully oxidized and then sent into the first absorbing device 4 through the mixing device 3; the first absorbent storage tank 18 and the second absorbent storage tank 19 respectively inject carbide slag and ammonia water into the circulating spray tank 11 of the second absorption device 7, a mixed absorbent formed in the circulating spray tank 11 is introduced into the spray device 6 of the first absorption device 4, the pH value of the mixed absorbent sprayed in the first absorption device 4 is controlled to be 6.5, oxidized flue gas is introduced from the top of the first absorption device 4, the flow rate of the flue gas is controlled to be 3.5m/s, and the flue gas is in countercurrent contact with the mixed absorbent sprayed by the spray device 6;
(2) the flue gas is discharged from the first absorption device 4 and enters a circulating spray area 8 of a second absorption device 7 through a flue, the pH value of a mixed absorbent circularly sprayed in the second absorption device 7 is controlled to be 5.3, the flow rate of the flue gas in the second absorption device 7 is controlled to be 3m/s, the mixed absorbent formed in a circulating spray pool 11 is circularly sprayed in the circulating spray area 8 and is in countercurrent contact with the flue gas, and the liquid-gas ratio of the mixed absorbent to the flue gas is 10: 1; the flue gas continuously rises to enter a first multi-effect spraying area 9, the carbide slag stored in a first desulfurizer storage tank is respectively introduced into a first injection device 13 and a first spraying device 14, the first injection device 13 and a second spraying device 16 spray the carbide slag oppositely, the flue gas is fully contacted with the carbide slag, and the liquid-gas ratio of the carbide slag to the flue gas is 8: 1; the flue gas continuously rises to enter a second multi-effect spraying area 10, ammonia water stored in a second desulfurizer storage tank is respectively introduced into a second injection device 15 and a second spraying device 16, the second injection device 15 and the second spraying device 16 spray the ammonia water oppositely, the flue gas is fully contacted with the ammonia water, and the liquid-gas ratio of the ammonia water to the flue gas is 5: 1; demisting the flue gas subjected to deep desulfurization and denitrification, and then discharging the demisted flue gas from the top of the second absorption device 7;
(3) with the proceeding of the spraying process in the second absorption device 7, the ineffective absorbent containing ammonium sulfate, ammonium nitrate and calcium sulfite is continuously formed in the circulating spraying pool 11, and when the solid content in the ineffective absorbent reaches 20%, the ineffective absorbent is discharged outside, and is sequentially separated by the cyclone separation device 20 and the centrifugal separation device 21 to obtain slurry and clear liquid; wherein, the clear liquid enters a drying device 22 for drying and dehydration to form ammonium sulfate and ammonium nitrate crystals; the slurry falls into an oxidation tank 23 to be in contact with air introduced by a blower 25 for oxidation, calcium sulfite in the slurry is converted into calcium sulfate, the oxidized slurry is filtered to obtain gypsum, and the filtrate returns to the oxidation tank 23 for recycling.
The purified flue gas discharged from the top of the second absorption device 7 was subjected to sampling test, and the desulfurization rate was calculated to be 95.2%, and the denitration rate was calculated to be 93.5%.
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 (10)
1. The desulfurization and denitrification system is characterized by comprising a first absorption device and a second absorption device which are sequentially communicated along the flow direction of flue gas;
an ozone generating device is connected into an inlet flue of the first absorption device;
the second absorption device is internally and sequentially divided into a circulating spraying area and at least two layers of multi-effect spraying areas from bottom to top along the flow direction of flue gas, the circulating spraying area is externally connected with at least two absorbent storage tanks, the absorbent storage tanks are respectively and independently connected into the multi-effect spraying areas, and the absorbent storage tanks respectively supply absorbent to the circulating spraying area and the multi-effect spraying areas;
the recycling spraying area is externally connected with a recycling unit, and the recycling unit is used for recycling the ineffective absorbent generated after spraying.
2. The desulfurization and denitrification system according to claim 1, wherein the ozone generating device is connected to the inlet flue through an ozone conveying pipeline;
the outlet end of the ozone conveying pipeline extends into the inlet flue;
the outlet end of the ozone conveying pipeline is provided with a distribution feeding device;
the spraying direction of the distribution feeding device is opposite to the flow direction of the flue gas, and the flue gas is in countercurrent contact with ozone after being introduced into the inlet flue;
along the flue gas flow direction, the inlet flue at the rear end of the ozone generating device is internally provided with a mixing device, and the flue gas is mixed and fully oxidized by the mixing device after contacting with the ozone.
3. The desulfurization and denitrification system according to claim 2, wherein the outlet end of the inlet flue is connected with the top flue gas inlet of the first absorption device, and flue gas is discharged from the inlet flue and then enters from the top of the first absorption device;
the bottom of the first absorption device is a liquid storage tank, at least two groups of spraying devices are arranged above the liquid storage tank side by side, and the absorbent sprayed by the spraying devices falls into the bottom of the first absorption device to form the liquid storage tank;
the spraying device comprises a spraying pipeline and nozzles uniformly distributed on the spraying pipeline, and the spraying direction of the nozzles is opposite to the flow direction of the flue gas;
and the bottom of the first absorption device is externally connected with a liquid discharge pipeline.
4. The desulfurization and denitrification system according to claim 3, wherein the interior of the second absorption device is divided into a circulating spray area, a first multi-effect spray area and a second multi-effect spray area from bottom to top in sequence along the flow direction of flue gas.
5. The desulfurization and denitrification system according to claim 4, wherein the circulating spray zone comprises a circulating spray tank and a circulating spray device positioned above the circulating spray tank, and the circulating spray tank is formed after the absorbent sprayed by the circulating spray device falls into the bottom of the second absorption device;
the circulating spray tank is connected with a circulating spray device through an external circulating spray pipeline;
the first absorption device is communicated with the second absorption device through a flue, flue gas is discharged by the first absorption device and then flows into the second absorption device through the flue, the inlet end of the flue is positioned between the liquid storage tank of the first absorption device and the spray device, and the outlet end of the flue is positioned between the circulating spray tank of the second absorption device and the circulating spray device;
the circulating spray tank is respectively and independently connected with a first absorbent storage tank and a second absorbent storage tank, and is also externally connected with a spray device of the first absorbent device;
and the liquid storage tank of the first absorption device is connected with the circulating spray tank of the second absorption device, and the liquid storage tank and the circulating spray tank are connected to realize liquid level balance.
6. The desulfurization and denitrification system according to claim 5, wherein the first absorbent storage tank stores a calcium-based absorbent, and the second absorbent storage tank stores ammonia water;
the first absorbent storage tank and the second absorbent storage tank respectively provide a calcium-based absorbent and ammonia water for the circulating spray pond.
7. The desulfurization and denitrification system according to claim 6, wherein the calcium-based absorbent is any one of quick lime, limestone, steel slag, papermaking white mud or carbide slag.
8. The desulfurization and denitrification system according to claim 7, wherein the first multi-effect spray zone comprises a first spraying device and a first spraying device positioned above the first spraying device;
the first absorbent storage tank is respectively and independently connected with the first injection device and the first spraying device, the first absorbent storage tank respectively provides calcium-based absorbent for the first injection device and the first spraying device, a desulfurization and denitrification space is formed between the first injection device and the first spraying device, and flue gas is contacted with the calcium-based absorbent in the desulfurization and denitrification space;
the spraying direction of the first spraying device is opposite to the spraying direction of the first spraying device;
the second multi-effect spraying area comprises a second spraying device and a second spraying device positioned above the second spraying device.
9. The desulfurization and denitrification system according to claim 8, wherein the second absorbent storage tank is independently connected to a second injection device and a second spray device, the second absorbent storage tank supplies ammonia water to the second injection device and the second spray device, a desulfurization and denitrification space is formed between the second injection device and the second spray device, and the flue gas is contacted with the ammonia water in the desulfurization and denitrification space;
the spraying direction of the second spraying device is opposite to the spraying direction of the second spraying device;
and a demisting device is also arranged at the smoke outlet of the second absorption device.
10. The desulfurization and denitrification system according to claim 9, wherein the recovery unit comprises a cyclone separation device, a centrifugal separation device, a drying device, an oxidation tank and a filtering device, the bottom of the circulating spray tank is sequentially connected with the cyclone separation device and the centrifugal separation device along the direction of the discharged absorbent, the discharge port of the centrifugal separation device is connected with the drying device, the liquid outlet of the centrifugal separation device is in butt joint with the oxidation tank, and the oxidation tank is in circulating connection with the filtering device;
the oxidation tank is also externally connected with an air blower.
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