CN100531867C - Method and apparatus for combined removing sulfur-dioxide and nitrogen oxide by mixed solution - Google Patents
Method and apparatus for combined removing sulfur-dioxide and nitrogen oxide by mixed solution Download PDFInfo
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Abstract
The invention is concerned with a method to remove sulfur dioxide and compounds of nitrogen and oxygen by using a kind of mixed solution. Drop the temperature of gas after moving dust to 100 to 110 degree, and contact with carbamide / ammonia mixed solution with additive to absorb sulfur dioxide and compounds of nitrogen and oxygen, then blow compressed air into the solution to get ammonia sulfate. Remove the solution and make gas contact with carbamide solution with additive, then let out after reaction. It can adopt double level spray or column reactor to coupling the first and second reactors into a same container and separate double lever reactor with clapboard, this predigests the connecting structure of double lever reactor and reduce the height of cleaning equipment and heat lost.
Description
Technical field
The invention belongs to the technical field of atmospheric environment protection, relate to a kind of flue gas and desulfurizing and denitrifying method and desulfuring and denitrifying apparatus, particularly relate to and a kind ofly utilize urea/ammoniacal liquor/additive mixed solution to unite to remove sulfur dioxide and nitrogen oxide method and device thereof.
Technical background
Sulfur dioxide and nitrogen oxide are the bigger gaseous contaminants of influence in the atmosphere pollution, human body, environment and the ecosystem are had very big harm, along with the increasingly stringent of environmental requirement, NO
XAnd SO
2The problem of discharging more and more receives publicity.Sulfur dioxide and nitrogen oxide mainly stem from the combustion process of fossil fuels such as coal, oil, and the fume emission of the roasting of ore, smelting process, wherein various burning boilers particularly power plant boiler smoke evacuation have characteristics such as concentration is low, exhaust gas volumn is big, floating dust is many and are difficult to improvement.In the conventional art, discharging sulfur dioxide in flue gas and purification of nitrogen oxides technology are normally separately carried out desulfurization and denitration, complicated huge, defectives such as initial outlay is big, operating cost height that this has caused the discharging flue gas purification system have seriously restricted the actual enforcement of discharging flue gas desulfurization and denitrification.Flue gas desulfurization technique is mainly based on limestone-gypsum wet method, rotating spraying semidry method, in-furnace calcium spraying afterbody humidification activation, sea water desulfuration, electron beam desulfurization, flue gas circulating fluidized bed desulfurization etc., wherein the wet type limestone-based process is the tail flue gas desulfur technology that is most widely used in the world now, its subject matter is that the solubility of absorbent (lime or lime stone) is little, utilization rate is low, and the waste residue amount is big; Gas denitrifying technology mainly contains SCR technology (SCR), SNCR technology (SNCR), electronic beam method, impulse electric corona method, complex compound absorption process and urea absorption process etc., comparatively ripe gas denitrifying technology at present in service mainly is SCR technology, SNCR technology and SNCR/SCR combination technique, but the SCR method exists the initial investment expense higher, operating temperature range is narrow, and exist ammonia to leak, can generate N
2O, and shortcoming such as the easy inactivation of catalyst; And the SNCR denitration efficiency is lower, and the ammonia leakage is many, causes secondary pollution.Countries in the world in recent years, especially industrially developed country has all carried out desulphurization denitration Study on Technology exploitation simultaneously in succession, and carried out certain commercial Application, electron beam irradiation method, impulse electric corona method, active carbon adsorption, NOxSO technology and Pahlman flue gas desulfurization and denitration technique etc. are abroad arranged at present, but China still lack at present this type of technology or because of energy consumption and cost too high and incompatible.Chinese invention patent (application number: 91105599.1) proposed to carry out desulphurization denitration with ammoniacal liquor, sulphur ammonium or its acidic aqueous solution, urea and compound powder thereof or its aqueous solution different high-temperature sections in stove.This invention and the present invention have some something in common on desulfurization denitrification agent, but it uses technology different fully with this law, the difference of serviceability temperature section especially, and its effect also differs widely.Chinese invention patent (application number: 91105599.1) be used for the furnace high-temperature section, certainly will bring high energy loss, and problem such as stove internal corrosion.Therefore, seek the flue gases purification of a kind of efficient, low-cost, low operating cost, non-secondary pollution, become the problem of China environmental protection researcher concern.
Summary of the invention
The present invention is intended to provide a kind of overall efficiency height, cost of investment is low, operating cost is little, the mixed solution of the low-temperature zone of non-secondary pollution is united and removed sulfur dioxide and nitrogen oxide method and device thereof.
The present invention adopts following technical scheme:
Mixed solution of the present invention is united and is removed sulfur dioxide and the nitrogen oxide method is as follows
The first step: with behind the flue gas cool-down to 100 after the dedusting ℃～110 ℃, make again flue gas with blending the urea of additive/ammoniacal liquor mixed solution carry out gas-liquid and contact, the liquid-gas ratio of mixed solution and flue gas is 1.5～4L/m
3, the concentration of ammoniacal liquor in mixed solution is 2%～10%, and the solution concentration of urea in mixed solution is 2%～6%, and mixed solution maintains 5～7 as one-level absorbent solution and its pH value, and temperature is controlled at 30 ℃～60 ℃, the SO in the flue gas
2With NO, be absorbed, sulfite oxidation is become ammonium sulfate contacting with flue gas and compressed air takes place to blast in the reacted solution, the addition of above-mentioned additive is 0.005%～0.025% mass percentage content of urea/ammonia spirit;
Second step: remove the solution of carrying secretly in the flue gas after one-level absorbs, make again this flue gas with blending the urea liquid of additive carry out gas-liquid and contact, reaction is finished the back and is discharged, the liquid-gas ratio of flue gas is 5～20L/m after above-mentioned urea liquid and the one-level absorption
3The mass concentration of urea in containing the solution of additive is 4%～13%, the solution that contains additive maintains 5.5～8 as secondary absorbent solution and its pH value, and temperature is controlled at 30 ℃～60 ℃, and the addition of additive is 0.005%～0.025% mass percent of urea liquid.
Of the present inventionly be used to implement mixed solution and unite the device that removes sulfur dioxide and nitrogen oxide method, be by heat exchanger, the one-level gas distributor, the one-level absorption reactor thermally, the one-level demister, the secondary gas distributor, the secondary absorption reactor thermally, the secondary demister, the secondary circulating pump, the secondary collecting tank, pump, centrifuge, the one-level collecting tank, separate liquid pump, air compressor machine, the one-level circulating pump is formed, the one-level gas distributor is located in the one-level absorption reactor thermally, the secondary gas distributor is located in the secondary absorption reactor thermally, the exhanst gas outlet of heat exchanger is connected with one-level absorption reactor thermally smoke inlet, the flue gas gas outlet of one-level absorption reactor thermally is connected with the smoke air inlet of secondary absorption reactor thermally, the one-level demister is between the smoke air inlet of the flue gas gas outlet of one-level absorption reactor thermally and secondary absorption reactor thermally, the secondary demister is located on the secondary absorption reactor thermally exhanst gas outlet, the one-level collecting tank is located at the below of one-level absorption reactor thermally, between the circulation fluid outlet that the one-level circulating pump is located at the one-level collecting tank and the inlet of one-level absorption reactor thermally and the one-level inlet of circulating pump be connected with the circulation fluid outlet of one-level collecting tank, the one-level outlet of circulating pump is connected with the inlet of one-level absorption reactor thermally, the secondary collecting tank is located at the below of secondary absorption reactor thermally, between the circulation fluid outlet that the secondary circulating pump is located at the secondary collecting tank and the inlet of secondary absorption reactor thermally and the secondary inlet of circulating pump be connected with secondary collecting tank circulation fluid outlet, the secondary outlet of circulating pump is connected with the inlet of secondary absorption reactor thermally, the ammonium sulfate crystallization solution outlet of one-level collecting tank is connected with the import of centrifuge, the liquid outlet of centrifuge is connected with the parting liquid pump inlet, the parting liquid pump discharge is connected with the import of one-level collecting tank, the outlet of air compressor machine is connected with the import of one-level collecting tank, and the dense ammonium sulfite solution outlet of secondary collecting tank is connected by the import of pump with the one-level collecting tank.
Of the present inventionly be used to implement mixed solution to unite a kind of improvement project of the device that removes sulfur dioxide and nitrogen oxide method be by heat exchanger, monoblock type one second reactor, the secondary demister, the secondary circulating pump, pump, centrifuge, separate liquid pump, air compressor machine, the one-level circulating pump is formed, monoblock type one second reactor comprises cylindrical shell, in cylindrical shell, be provided with dividing plate and be the one-level absorption reactor thermally by the space that this dividing plate and cylindrical shell surround, another space that is surrounded by this dividing plate and cylindrical shell is the secondary absorption reactor thermally, on the one-level absorption reactor thermally, be provided with one-level absorption reactor thermally smoke inlet, be provided with the one-level gas distributor in the bottom of one-level absorption reactor thermally, be connected with the one-level collecting tank in the lower end of one-level absorption reactor thermally, be provided with the one-level demister on the top of one-level absorption reactor thermally, in the one-level absorption reactor thermally and be positioned at the one-level demister below be provided with the one-level spray thrower, and the nozzle of one-level spray thrower is downward, on the secondary absorption reactor thermally, be provided with secondary absorption reactor thermally exhanst gas outlet, be connected with the secondary collecting tank in the lower end of secondary absorption reactor thermally, be provided with the secondary gas distributor on the top of secondary absorption reactor thermally, in the secondary absorption reactor thermally and to be positioned at the nozzle that is provided with secondary spray thrower and secondary spray thrower below the secondary gas distributor downward, one-level demister and secondary gas distributor are by channel connection, the exhanst gas outlet of above-mentioned heat exchanger is connected with one-level absorption reactor thermally smoke inlet, the secondary demister is located on the secondary absorption reactor thermally exhanst gas outlet, between the circulation fluid outlet that the one-level circulating pump is located at the one-level collecting tank and the inlet of one-level spray thrower and the one-level inlet of circulating pump be connected with the circulation fluid outlet of one-level collecting tank, the one-level outlet of circulating pump is connected with the inlet of one-level spray thrower, between the circulation fluid outlet that the secondary circulating pump is located at the secondary collecting tank and the inlet of secondary spray thrower and the secondary inlet of circulating pump be connected with secondary collecting tank circulation fluid outlet, the secondary outlet of circulating pump is connected with the inlet of secondary spray thrower, the secondary outlet of circulating pump is connected with the inlet of secondary absorption reactor thermally, the ammonium sulfate crystallization solution outlet of one-level collecting tank is connected with the import of centrifuge, the liquid outlet of centrifuge is connected with the parting liquid pump inlet, the parting liquid pump discharge is connected with the import of one-level collecting tank, the outlet of air compressor machine is connected with the import of one-level collecting tank, and the dense ammonium sulfite solution outlet of secondary collecting tank is connected by the import of pump with the one-level collecting tank.
Of the present inventionly be used to implement mixed solution to unite the another kind of scheme of the device that removes sulfur dioxide and nitrogen oxide method be by heat exchanger, monoblock type one second reactor, the secondary demister, the secondary circulating pump, pump, centrifuge, separate liquid pump, air compressor machine, the one-level circulating pump is formed, monoblock type one second reactor comprises cylindrical shell, in cylindrical shell, be provided with dividing plate and be the one-level absorption reactor thermally by the space that this dividing plate and cylindrical shell surround, another space that is surrounded by this dividing plate and cylindrical shell is the secondary absorption reactor thermally, on the one-level absorption reactor thermally, be provided with one-level absorption reactor thermally smoke inlet, be provided with the one-level gas distributor in the bottom of one-level absorption reactor thermally, be connected with the one-level collecting tank in the lower end of one-level absorption reactor thermally, be provided with the one-level demister on the top of one-level absorption reactor thermally, be provided with one-level fluid column formula injector in one-level absorption reactor thermally bottom and above being positioned at the one-level gas distributor, and the nozzle of one-level fluid column formula injector upwards, on the secondary absorption reactor thermally, be provided with secondary absorption reactor thermally exhanst gas outlet, be connected with the secondary collecting tank in the lower end of secondary absorption reactor thermally, be provided with the secondary gas distributor on the top of secondary absorption reactor thermally, the nozzle that is provided with secondary fluid column formula injector and secondary fluid column formula injector in the bottom of secondary absorption reactor thermally makes progress, one-level demister and secondary gas distributor are by channel connection, the exhanst gas outlet of above-mentioned heat exchanger is connected with one-level absorption reactor thermally smoke inlet, the secondary demister is located on the secondary absorption reactor thermally exhanst gas outlet, between the circulation fluid outlet that the one-level circulating pump is located at the one-level collecting tank and the inlet of one-level fluid column formula injector and the one-level inlet of circulating pump be connected with the circulation fluid outlet of one-level collecting tank, the one-level outlet of circulating pump is connected with the inlet of one-level fluid column formula injector, between the circulation fluid outlet that the secondary circulating pump is located at the secondary collecting tank and the inlet of secondary fluid column formula injector and the secondary inlet of circulating pump be connected with secondary collecting tank circulation fluid outlet, the secondary outlet of circulating pump is connected with the inlet of secondary fluid column formula injector, the secondary outlet of circulating pump is connected with the inlet of secondary absorption reactor thermally (6), the ammonium sulfate crystallization solution outlet of one-level collecting tank is connected with the import of centrifuge, the liquid outlet of centrifuge is connected with the parting liquid pump inlet, the parting liquid pump discharge is connected with the import of one-level collecting tank, the outlet of air compressor machine is connected with the import of one-level collecting tank, and the dense ammonium sulfite solution outlet of secondary collecting tank is connected by the import of pump with the one-level collecting tank.
The course of work of the present invention is as follows: the flue gas after the dedusting enters the A reactor main body through pipeline again after pipeline enters the heat exchanger cooling, flue gas evenly enters the one-level absorption reactor thermally through the one-level gas distributor earlier in the A reactor main body; Circulating absorption solution is pumped in the one-level absorption reactor thermally by the one-level circulating pump through pipeline in the one-level collecting tank; Ammonia spirit in the ammoniacal liquor liquid pool is pumped into the pipeline that is connected with air compressor machine through pipeline by aqua ammonia pump, in compressed air is sent into the one-level collecting tank, the ammonium sulfate of one-level collecting tank inner bottom part crystallization is through pipeline, enter centrifuge through valve again, separate obtaining 98% ammonia sulfate crystal, the solution after centrifuge separates pumps in the one-level collecting tank by separating liquid pump through pipeline; Flue gas behind the first class purification enters the second reactor main body through the one-level demister, and flue gas enters the secondary absorption reactor thermally again through the secondary gas distributor earlier; Circulating absorption solution in the secondary collecting tank is pumped in the secondary absorption reactor thermally by the secondary circulating pump through pipeline; Urea liquid in the urea liquid liquid pool is sent into the pipeline that is connected with the secondary circulating pump by urea solution pump through pipeline, in circulation fluid is sent into the secondary absorption reactor thermally; When circulating absorption solution reaches certain ammonium sulfate concentrations in the secondary collecting tank, pump into the pipeline that is connected with air compressor machine through pipeline by pump, in compressed air is sent into the one-level collecting tank; Flue gas behind the secondary purification passes through the secondary demister again, enters heat exchanger by pipeline and heats up the back by in the pipeline feeding chimney.
Compared with prior art, the present invention has following advantage:
The present invention is a kind of wet method urea/ammoniacal liquor/additive solution flue gas and desulfurizing and denitrifying technology, adopt urea/ammonia spirit as the while desulfurization denitrification agent, with triethanolamine, ethylenediamine etc. as additive, flue gas and absorption liquid carry out gas-liquid mixed in the two-stage reaction tower, realize desulphurization denitration process simultaneously effectively, absorption liquid makes byproduct of ammonium sulfate through oxidation again, this technology has overcome the shortcoming of conventional flue gas purifying technique function singleness, and its overall efficiency height, system is simple, cost of investment is low, operating cost is little, non-secondary pollution.
Basic process is as follows:
Contain at first enter heat exchanger after pollution flue gas (about about the 160 ℃) dedusting of sulfur dioxide and nitrogen oxide and be cooled to 100 ℃～110 ℃ after, enter the A reactor main body, flue gas through gas distributor enter the one-level absorption reactor thermally with blending additives such as triethanolamine or ethylenediamine (additive add mass percent be urea/ammonia spirit 0.005%～0.025%) urea/ammoniacal liquor mixed solution (primary amine concentration of aqueous solution be 2%～10% be 2%～6% with urea concentration) carry out gas-liquid mixed and contact, the pH value of absorbent solution maintains 5～7, temperature is controlled at 30 ℃～60 ℃, the SO in the flue gas
2And NO
xAbsorbed simultaneously; Simultaneously blast compressed air sulfite oxidation is become ammonium sulfate to the collecting tank of A reactor main body; Flue gas behind the first class purification is removed flue gas through demister and is carried solution secretly, enter again in the second reactor main body, flue gas enters the secondary absorption reactor thermally through gas distributor again, once more with blending additives such as triethanolamine or ethylenediamine (additive add mass percent be urea liquid 0.005%～0.025%) urea liquid (urea quality concentration is 4～13%) carry out gas-liquid mixed and contact, the pH value of absorbent solution maintains 5.5～8, temperature is controlled at 30 ℃～60 ℃, the SO in the flue gas
2And NO
xRemoved once more, on a small quantity from the ammonia of one-level absorption reactor thermally at this by complete reaction, satisfy the discharge index of ammonia; Flue gas behind the secondary purification after demister is removed the liquid of carrying secretly (flue-gas temperature is 55 ℃～70 ℃) in the flue gas, is warming up to 75 ℃～90 ℃ through heat exchanger and enters atmosphere again.SO in this method flue gas
2Total removal efficiency is 90%～99%, NO
xTotal removal efficiency is 60%～85%, has reclaimed byproduct of ammonium sulfate simultaneously, there is no the secondary pollution deposits yields.
Make additive with triethanolamine, ethylenediamine etc., the principle of urea liquid or urea and ammonia spirit while desulphurization denitration is as follows:
Ammonia and SO
2And NO
xReaction:
SO
2+2NH
3+H
2O→(NH
4)
2SO
3 (1)
(NH
4)
2SO
3+SO
2+H
2O→2NH
4HSO
3 (2)
NH
4HSO
3+NH
3→(NH
4)
2SO
3 (3)
2(NH
4)
2SO
3+O
2→2(NH
4)
2SO
4 (4)
4(NH
4)
2SO
3+2NO
2→4(NH
4)
2SO
4+N
2 (5)
2(NH
4)
2SO
3+2NO→2(NH
4)
2SO
4+N
2 (6)
2(NH
4)OH+NO+NO
2→2NH
4NO
2+H
2O (7)
2NH
4NO
2→2N
2+4H
2O (8)
Because in the general flue gas, the oxidizability of nitrogen oxide is generally 5%～10%, reaction equation (5) and (6) denitration efficiency are very little, and because NH
4HSO
3Existence be unfavorable for (NH
4)
2SO
3To NO
xAbsorb, simultaneously NH
4HSO
3Reaction equation (7) there is inhibitory action.
Urea and SO
2And NO
xReaction:
2NO+O
2→2NO
2 (9)
Different component can be absorbed into liquid phase, and (Henry's constant of NO in water is very little, under the normal pressure, has only 1.25*10 in the time of 50 ℃ except the NO
-3Mol/L).React as follows:
By reacting (16) HNO as can be seen
2Decomposition can cause the generation of NO, and urea meeting and HNO
2Reaction generates N
2And CO
2, the generation of inhibitory reaction (16).React as follows:
CO(NH
2)
2+2HNO
2→2N
2+CO
2+3H
2O (17)
The reaction that absorbent urea and flue gas take place can be represented by following chemical equation:
NO(g)+NO
2(g)+(NH
2)
2CO(a.q)＝2H
2O(l)+CO
2(g)+2N
2(g) (18)
SO
2(g)+(NH
2)
2CO(a.q)+2H
2O(l)+0.5O
2(g)＝(NH
4)
2SO
4(a.q)+CO
2(g)?(19)
Make additive with triethanolamine, ethylenediamine etc., urea liquid or urea and ammonia spirit are made absorption/reducing agent, flue gas is carried out in the process of while desulphurization denitration, not only urea and ammonia have corresponding separately desulphurization denitration effect, and their intermediate product also has collaborative facilitation, the SO in the while flue gas
2And NO
xAlso have synergistic function, this has quickened the chemical reaction rate in the course of reaction greatly, has also just greatly improved gas cleaning efficient.
Additive such as triethanolamine, ethylenediamine mainly plays catalysis and buffering effect in course of reaction.Catalytic action is meant accelerated reaction speed or suppresses side reaction control the Direction of Reaction and process take place; Cushioning effect is meant regulates the absorption liquid pH value, makes absorption liquid trend alkalescent direction, prevents the corrosion of equipment.
Compare with conventional art, urea/ammonia of the present invention/additive solution is united the method that removes sulfur dioxide in flue gas and nitrogen oxide and is had following concrete advantage:
1. applied widely, this process and equipment can be used for all kinds of SO of containing
2And NO
xTail gas and the removing of flue gas, comprise boiler for domestic, Industrial Boiler, Industrial Stoves, station boiler, metallurgical tail gas, chemical industry tail gas; SO to high and low concentration
2And NO
xFlue gas all can effectively be removed.
2. adopt urea/ammonia/additive solution associating to remove the method for sulfur dioxide in flue gas and nitrogen oxide simultaneously, mixing contacts SO in the flue gas to flue gas with the urea mixed solution with ammonia in the A reactor
2Intermediate product (the NH that reaction generates with ammoniacal liquor
4)
2SO
3To NO
xHas decomposition (reaction (5) and (6)), intermediate product (NH4)
2SO
3Unite NO in the absorbing and removing flue gas together with urea
x, and process and speed that urea also can accelerated reaction (8) have not only improved absorbent solution to SO in the flue gas
2Removal efficiency, and strengthen and improved absorbent solution greatly to NO in the flue gas
xThe ability that removes.In the while flue gas and desulfurizing and denitrifying process, SO
2And NO
xAlso have collaborative facilitation, help the purification of flue gas.This method synthesis efficient height, SO
2Total removal efficiency is 90%～99%, NO
xTotal removal efficiency is 60%～85%, and its combination property can compare favourably with at present popular desulfurization of wet type limestone-based process and SCR method denitration combination, has reclaimed byproduct of ammonium sulfate simultaneously.
3. this urea/ammonia/additive solution associating removes the method for sulfur dioxide in flue gas and nitrogen oxide simultaneously, adopts flue gas and desulfurizing and denitrifying to carry out in low-temperature zone, makes the entire system efficiency of utilization improve, and has reduced energy consumption.
4. this urea/ammonia/additive solution is united the method that removes while sulfur dioxide in flue gas and nitrogen oxide, adopt additives such as cheap triethanolamine, ethylenediamine, not only reduced system operation cost, and had catalysis and buffering effect, quickened absorbent solution SO
2And NO
xReaction rate, and make absorption liquid trend alkalescent direction, prevented the corrosion of system equipment.
5. this urea/ammonia/additive solution low temperature associating removes the method for sulfur dioxide in flue gas and nitrogen oxide simultaneously, desulfurization and denitrating system are organically combined, this flue gas and desulfurizing and denitrifying system compares with SCR method denitration combination with at present popular wet type limestone-based process desulfurization and has obtained simplifying greatly, has saved initial outlay cost and operating cost.
6. adopt urea/ammonia/additive solution low temperature associating to remove the method for sulfur dioxide in flue gas and nitrogen oxide simultaneously, its product is the solubility height in water, and is less scaling, and security of operation is easy to maintenance, is easy to control; Because this method has been avoided scale problems, and the reactor inlet section can adopt suitable gas distributor, this has improved the uniformity of flue gas in reactor greatly, has improved system's gas cleaning efficient simultaneously.
7. this urea/ammonia/additive solution low temperature associating removes the method for sulfur dioxide in flue gas and nitrogen oxide simultaneously, adopts the two-stage reactor processing procedure, and mixing contacts most of SO in the flue gas to flue gas with the urea mixed solution with ammonia in A reactor
2And NO
xBy the associating absorbing and removing, flue gas is removed most drop in the flue gas through the one-level demister, and the ammonia of carrying secretly on a small quantity enters second reactor with flue gas; Flue gas only mixes with urea liquid and contacts in second reactor, the little ammonia that flue gas is carried secretly from A reactor this once more with flue gas SO
2Reaction, amino originally are consumed to the greatest extent, and the bi-level treatment process makes reaction temperature be easier to control, solve problems such as aerosol that the ammonia process of desulfurization causes and emission intensity effectively.
8. this urea/ammonia/additive solution low temperature associating removes the method for sulfur dioxide in flue gas and nitrogen oxide simultaneously, owing to adopt the bi-level treatment process, and can be to the SO of high and low variable concentrations
2And NO
xFlue gas adopts the ammonia and the urea mixed solution of different proportion, is convenient to adjusting in service and control, makes flue gas and desulfurizing and denitrifying efficient and operating cost reach economic optimum.
9. the method that adopts urea/ammonia/additive solution low temperature associating to remove sulfur dioxide in flue gas and nitrogen oxide has simultaneously realized the non-secondary pollution discharging, helps environmental protection.
10. adopt the two-stage reactor integrated design technology, one-level, second reactor are coupling in the same container, with dividing plate two-stage reactor is separated, make the outlet and the second reactor import of A reactor become the inner passage, the flow of flue gas direction becomes earlier the upwards downward again type of flow, this has not only simplified the connection structure of two-stage reactor greatly, reduced the height of flue gas purifying equipment, save the initial cost cost, reduced the device space, and reduced the radiation loss of flue gas purifying equipment, and reduced the pressure of follow-up intensification, saved the energy; In addition, realized that also flue gas hangs down the structural configuration of into hanging down, reduced the height of follow-up flue, saved cost, and helped the I﹠M of equipment.
Description of drawings
Fig. 1 is that urea/ammoniacal liquor of the present invention/additive solution associating removes the system flow chart of sulfur dioxide in flue gas and nitrogen oxide simultaneously, heat exchanger 1, one-level gas distributor 2, one-level absorption reactor thermally 3, one-level demister 4, secondary gas distributor 5, secondary absorption reactor thermally 6, secondary demister 7, urea solution pump 8, urea liquid Agitation Tank 9, secondary circulating pump 10, secondary collecting tank 11, pump 12, centrifuge 13, valve 14, one-level collecting tank 15 is wherein arranged, separate liquid pump 16, air compressor machine 17, one-level circulating pump 18, aqua ammonia pump 19, ammoniacal liquor Agitation Tank 20.
Fig. 2 is the structural representation of one-level of the present invention, secondary fountain absorption reactor thermally embodiment, and one-level absorption reactor thermally smoke inlet 21, one-level gas distributor 2, one-level spray thrower 22, one-level demister 4, firsts and seconds reactor dividing plate 23, secondary gas distributor 5, secondary spray thrower 24, secondary demister 7, secondary absorption reactor thermally exhanst gas outlet 25, reactor shell 28 are wherein arranged.
Fig. 3 is the structural representation of one-level of the present invention, secondary fluid column formula absorption reactor thermally embodiment, and one-level absorption reactor thermally smoke inlet 21, one-level gas distributor 2, one-level liquid column-spraying device 26, one-level demister 4, firsts and seconds reactor dividing plate 23, secondary gas distributor 5, secondary liquid column-spraying device 27, secondary demister 7, secondary absorption reactor thermally exhanst gas outlet 25, reactor shell 28 are wherein arranged.
The specific embodiment
Embodiment 1:
Describe urea/ammonia of the present invention/additive solution in detail with reference to Fig. 1 and unite the embodiment that removes sulfur dioxide in flue gas and nitrogen oxide method.
Contain sulfur dioxide 600mg/Nm
3～6000mg/Nm
3With nitrogen oxide 400mg/Nm
3～3000mg/Nm
3The about 160 ℃ of dedustings of flue gas after, after pipeline enters heat exchanger 1 and is cooled to 100～110 ℃, enter the A reactor main body; Flue gas earlier through one-level gas distributor 2 evenly enter one-level absorption reactor thermally 3 with blending additives adding mass percents such as triethanolamine or ethylenediamine be that urea/ammoniacal liquor mixed solution primary amine concentration of aqueous solution of 0.005%～0.025% of urea/ammonia spirit is 2%～10% to be 2%～6% to carry out gas-liquid mixed and contact most SO with urea concentration
2Be absorbed at this and remove part NO
xBe absorbed and remove; One-level absorption reactor thermally 3 can be spray column, packed tower or liquid column tower; The circulation absorbent solution pH value of A reactor main body maintains 5～7, and temperature is controlled at 30 ℃～60 ℃, and liquid-gas ratio is 1.5～4L/m
3, the flue gas superficial linear velocity in a column is controlled at 2.5～4m/s; Ammonia spirit in the ammoniacal liquor liquid pool 20 is pumped in the one-level collecting tank 15 by aqua ammonia pump 19; Circulating absorption solution in the one-level collecting tank 15 is squeezed in the one-level absorption reactor thermally 3 by one-level circulating pump 18, carries out recycling; Air compressor machine 17 blasts compressed air to one-level collecting tank 15 and will react the sulfite oxidation that generates and become ammonium sulfate, the ammonium sulfate of one-level collecting tank 15 intercrystallines is deposited on the bottom, after reaching finite concentration, enter centrifuge 13 through valves 14 and carry out Separation of Solid and Liquid, obtain 98% ammonia sulfate crystal, the solution after the separation is in pump 16 pumps into one-level collecting tank 15; Remove through one-level demister 4 again through the flue gas behind the first class purification and to carry solution (prevent ammonia from bringing secondary absorption reactor thermally main body in a large number into) in the flue gas secretly, flue gas from the A reactor main body evenly enters in the secondary absorption reactor thermally 6 flue gas through secondary gas distributor 5, once more with blending additives such as triethanolamine or ethylenediamine (additive add mass percent be urea liquid 0.005%～0.025%) urea liquid (urea quality concentration is 4～13%) carry out gas-liquid mixed and contact the SO in the flue gas
2And NO
xQuilt is absorbing and removing once more, and the little ammonia of carrying secretly from the flue gas of A reactor main body also has been fully utilized at this, satisfies the discharge index of ammonia fully; Secondary absorption reactor thermally 6 can be spray column, packed tower or liquid column tower; The absorbent solution pH value that circulates this moment maintains 5.5～8, and temperature is controlled at 30 ℃～60 ℃, and liquid-gas ratio is 5～20L/m
3, the flue gas superficial linear velocity in a column is controlled at 2.5～4m/s; Circulating absorption solution is squeezed in the secondary absorption reactor thermally 6 by secondary circulating pump 10 in the secondary collecting tank 11, carries out recycling; Urea liquid in the urea liquid liquid pool 9 is pumped in the secondary absorption reactor thermally 6 by urea solution pump 8; When circulating absorption solutions reach certain ammonium sulfate concentrations in the secondary collecting tank 11, pump in the one-level collecting tank 15 by pump 12; Flue gas behind the secondary purification enters chimney through the entrained liquids (flue-gas temperature is 55 ℃～70 ℃) that secondary demister 7 is removed in the flue gas after heat exchanger 1 is warming up to 75 ℃～90 ℃ again.SO behind the two-stage absorbing and removing
2Total removal efficiency is 90%～99%, NO
xTotal removal efficiency is 60%～85%, has reclaimed byproduct of ammonium sulfate simultaneously, and whole system realizes recycling, the non-secondary pollution deposits yields.
Embodiment 2: mixed solution disclosed by the invention is united and is removed sulfur dioxide and the nitrogen oxide method is as follows:
The first step: with behind the flue gas cool-down to 100 after the dedusting ℃～110 ℃, make again flue gas with blending the urea of additive/ammoniacal liquor mixed solution carry out gas-liquid and contact, the liquid-gas ratio of mixed solution and flue gas is 1.5～4L/m
3, the concentration of ammoniacal liquor in mixed solution is 2%～10%, and the solution concentration of urea in mixed solution is 2%～6%, and mixed solution maintains 5～7 as one-level absorbent solution and its pH value, and temperature is controlled at 30 ℃～60 ℃, the SO in the flue gas
2And NO
xBe absorbed, sulfite oxidation become ammonium sulfate contacting with flue gas and compressed air takes place to blast in the reacted solution, the addition of above-mentioned additive is 0.005%～0.025% mass percentage content of urea/ammonia spirit;
Second step: remove the solution of carrying secretly in the flue gas after one-level absorbs, make again this flue gas with blending the urea liquid of additive carry out gas-liquid and contact, reaction is finished the back and is discharged, the liquid-gas ratio of flue gas is 5～20L/m after above-mentioned urea liquid and the one-level absorption
3The mass concentration of urea in containing the solution of additive is 4%～13%, the solution that contains additive maintains 5.5～8 as secondary absorbent solution and its pH value, and temperature is controlled at 30 ℃～60 ℃, and the addition of additive is 0.005%～0.025% mass percent of urea liquid.
Above-mentioned mixed solution unite remove sulfur dioxide and nitrogen oxide method wherein additive be one or more mixture in triethanolamine, ethylenediamine, the phosphamide.
Above-mentioned mixed solution is united the flue gas that removes in sulfur dioxide and the nitrogen oxide method after secondary absorbs, and discharges after demister is removed the liquid of carrying secretly in the flue gas.
Embodiment 3: a kind ofly be used to implement described mixed solution to unite the device that removes sulfur dioxide and nitrogen oxide method be by heat exchanger 1, one-level gas distributor 2, one-level absorption reactor thermally 3, one-level demister 4, secondary gas distributor 5, secondary absorption reactor thermally 6, secondary demister 7, secondary circulating pump 10, secondary collecting tank 11, pump 12, centrifuge 13, one-level collecting tank 15, separate liquid pump 16, air compressor machine 17, one-level circulating pump 18 is formed, one-level gas distributor 2 is located in the one-level absorption reactor thermally 3, secondary gas distributor 5 is located in the secondary absorption reactor thermally 6, the exhanst gas outlet of heat exchanger 1 is connected with one-level absorption reactor thermally smoke inlet 21, the flue gas gas outlet of one-level absorption reactor thermally 3 is connected with the smoke air inlet of secondary absorption reactor thermally 6, one-level demister 4 is between the smoke air inlet of the flue gas gas outlet of one-level absorption reactor thermally 3 and secondary absorption reactor thermally 6, secondary demister 7 is located on the secondary absorption reactor thermally exhanst gas outlet 25, one-level collecting tank 15 is located at the below of one-level absorption reactor thermally 3, between the circulation fluid outlet that one-level circulating pump 18 is located at one-level collecting tank 15 and the inlet of one-level absorption reactor thermally 3 and the import of one-level circulating pump 18 be connected with the circulation fluid outlet of one-level collecting tank 15, the outlet of one-level circulating pump 18 is connected with the inlet of one-level absorption reactor thermally 3, secondary collecting tank 11 is located at the below of secondary absorption reactor thermally 6, between the circulation fluid outlet that secondary circulating pump 10 is located at secondary collecting tank 11 and the inlet of secondary absorption reactor thermally 6 and the import of secondary circulating pump 10 be connected with secondary collecting tank 11 circulation fluid outlets, the outlet of secondary circulating pump 10 is connected with the inlet of secondary absorption reactor thermally 6, the ammonium sulfate crystallization solution outlet of one-level collecting tank 15 is connected with the import of centrifuge 13, the liquid outlet of centrifuge 13 with separate liquid pump 16 imports and be connected, separating liquid pump 16 outlets is connected with the import of one-level collecting tank 15, the outlet of air compressor machine 17 is connected with the import of one-level collecting tank 15, and the dense ammonium sulfite solution outlet of secondary collecting tank 11 is connected with the import of one-level collecting tank 15 by pump 12.
Described device is connected with aqua ammonia pump 19 and one-level collecting tank 15 in the import of one-level collecting tank 15 import is connected with the outlet of aqua ammonia pump 19, and the import that is connected with ammoniacal liquor Agitation Tank 20 and aqua ammonia pump 19 on aqua ammonia pump 19 is connected with the outlet of ammoniacal liquor Agitation Tank 20.
Above-mentioned device is connected with urea solution pump 8 and one-level collecting tank 15 in the import of one-level collecting tank 15 import is connected with the outlet of urea solution pump 8, and the import that is connected with urea liquid Agitation Tank 9 and urea solution pump 8 on urea solution pump 8 is connected with the outlet of urea liquid Agitation Tank 9.
Described device is provided with valve 14 between the import of the ammonium sulfate crystallization solution outlet of one-level collecting tank 15 and centrifuge 13.
The low-temperature flue gas import after the purification of secondary absorption reactor thermally exhanst gas outlet 25 and heat exchanger 1 of described device is connected.
Embodiment 4:
With reference to Fig. 2, a kind ofly be used to implement described mixed solution to unite the device that removes sulfur dioxide and nitrogen oxide method be by heat exchanger 1, monoblock type one second reactor, secondary demister 7, secondary circulating pump 10, pump 12, centrifuge 13, separate liquid pump 16, air compressor machine 17, one-level circulating pump 18 is formed, monoblock type one second reactor comprises cylindrical shell 28, a space that is provided with dividing plate 23 and is surrounded by this dividing plate 23 and cylindrical shell 28 in cylindrical shell 28 is an one-level absorption reactor thermally 3, is secondary absorption reactor thermally 6 by this dividing plate 23 with another space that cylindrical shell 28 surrounds, on one-level absorption reactor thermally 3, be provided with one-level absorption reactor thermally smoke inlet 21, be provided with one-level gas distributor 2 in the bottom of one-level absorption reactor thermally 3, be connected with one-level collecting tank 15 in the lower end of one-level absorption reactor thermally 3, be provided with one-level demister 4 on the top of one-level absorption reactor thermally 3, in one-level absorption reactor thermally 3 and be positioned at one-level demister 4 below be provided with one-level spray thrower 22, and the nozzle of one-level spray thrower 22 is downward, on secondary absorption reactor thermally 6, be provided with secondary absorption reactor thermally exhanst gas outlet 25, be connected with secondary collecting tank 11 in the lower end of secondary absorption reactor thermally 6, be provided with secondary gas distributor 5 on the top of secondary absorption reactor thermally 6, in secondary absorption reactor thermally 6 and to be positioned at the nozzle that is provided with secondary spray thrower 24 and secondary spray thrower 24 below the secondary gas distributor 5 downward, one-level demister 4 and secondary gas distributor 5 are by channel connection, the exhanst gas outlet of above-mentioned heat exchanger 1 is connected with one-level absorption reactor thermally smoke inlet 21, secondary demister 7 is located on the secondary absorption reactor thermally exhanst gas outlet 25, between the circulation fluid outlet that one-level circulating pump 18 is located at one-level collecting tank 15 and the inlet of one-level spray thrower 22 and the import of one-level circulating pump 18 be connected with the circulation fluid outlet of one-level collecting tank 15, the outlet of one-level circulating pump 18 is connected with the inlet of one-level spray thrower 22, between the circulation fluid outlet that secondary circulating pump 10 is located at secondary collecting tank 11 and the inlet of secondary spray thrower 24 and the import of secondary circulating pump 10 be connected with secondary collecting tank 11 circulation fluid outlets, the outlet of secondary circulating pump 10 is connected with the inlet of secondary spray thrower 24, the outlet of secondary circulating pump 10 is connected with the inlet of secondary absorption reactor thermally 6, the ammonium sulfate crystallization solution outlet of one-level collecting tank 15 is connected with the import of centrifuge 13, the liquid outlet of centrifuge 13 with separate liquid pump 16 imports and be connected, separating liquid pump 16 outlets is connected with the import of one-level collecting tank 15, the outlet of air compressor machine 17 is connected with the import of one-level collecting tank 15, and the dense ammonium sulfite solution outlet of secondary collecting tank 11 is connected with the import of one-level collecting tank 15 by pump 12.。
Embodiment 5:
With reference to Fig. 3, a kind ofly be used for described mixed solution and unite the device that removes sulfur dioxide and nitrogen oxide method, be by heat exchanger 1, monoblock type one second reactor, secondary demister 7, secondary circulating pump 10, pump 12, centrifuge 13, separate liquid pump 16, air compressor machine 17, one-level circulating pump 18 is formed, monoblock type one second reactor comprises cylindrical shell 28, a space that is provided with dividing plate 23 and is surrounded by this dividing plate 23 and cylindrical shell 28 in cylindrical shell 28 is an one-level absorption reactor thermally 3, is secondary absorption reactor thermally 6 by this dividing plate 23 with another space that cylindrical shell 28 surrounds, on one-level absorption reactor thermally 3, be provided with one-level absorption reactor thermally smoke inlet 21, be provided with one-level gas distributor 2 in the bottom of one-level absorption reactor thermally 3, be connected with one-level collecting tank 15 in the lower end of one-level absorption reactor thermally 3, be provided with one-level demister 4 on the top of one-level absorption reactor thermally 3, be provided with one-level fluid column formula injector 26 in one-level absorption reactor thermally 3 bottoms and above being positioned at one-level gas distributor 2, and the nozzle of one-level fluid column formula injector 26 upwards, on secondary absorption reactor thermally 6, be provided with secondary absorption reactor thermally exhanst gas outlet 25, be connected with secondary collecting tank 11 in the lower end of secondary absorption reactor thermally 6, be provided with secondary gas distributor 5 on the top of secondary absorption reactor thermally 6, the nozzle that is provided with secondary fluid column formula injector 27 and secondary fluid column formula injector 27 in the bottom of secondary absorption reactor thermally 6 makes progress, one-level demister 4 and secondary gas distributor 5 are by channel connection, the exhanst gas outlet of above-mentioned heat exchanger 1 is connected with one-level absorption reactor thermally smoke inlet 21, secondary demister 7 is located on the secondary absorption reactor thermally exhanst gas outlet 25, between the circulation fluid outlet that one-level circulating pump 18 is located at one-level collecting tank 15 and the inlet of one-level fluid column formula injector 26 and the import of one-level circulating pump 18 be connected with the circulation fluid outlet of one-level collecting tank 15, the outlet of one-level circulating pump 18 is connected with the inlet of one-level fluid column formula injector 26, between the circulation fluid outlet that secondary circulating pump 10 is located at secondary collecting tank 11 and the inlet of secondary fluid column formula injector 27 and the import of secondary circulating pump 10 be connected with secondary collecting tank 11 circulation fluid outlets, the outlet of secondary circulating pump 10 is connected with the inlet of secondary fluid column formula injector 27, the outlet of secondary circulating pump 10 is connected with the inlet of secondary absorption reactor thermally 6, the ammonium sulfate crystallization solution outlet of one-level collecting tank 15 is connected with the import of centrifuge 13, the liquid outlet of centrifuge 13 with separate liquid pump 16 imports and be connected, separating liquid pump 16 outlets is connected with the import of one-level collecting tank 15, the outlet of air compressor machine 17 is connected with the import of one-level collecting tank 15, and the dense ammonium sulfite solution outlet of secondary collecting tank 11 is connected with the import of one-level collecting tank 15 by pump 12.
Claims (9)
1, a kind of mixed solution is united and is removed sulfur dioxide and nitrogen oxide method, it is characterized in that:
The first step: with behind the flue gas cool-down to 100 after the dedusting ℃～110 ℃, make again flue gas with blending the urea of additive/ammoniacal liquor mixed solution carry out gas-liquid and contact, the liquid-gas ratio of mixed solution and flue gas is 1.5～4L/m
3, the concentration of ammoniacal liquor in mixed solution is 2%～10%, and the solution concentration of urea in mixed solution is 2%～6%, and mixed solution maintains 5～7 as one-level absorbent solution and its pH value, and temperature is controlled at 30 ℃～60 ℃, the SO in the flue gas
2And NO
xBe absorbed, sulfite oxidation become ammonium sulfate contacting with flue gas and compressed air takes place to blast in the reacted solution, the addition of above-mentioned additive is 0.005%～0.025% mass percentage content of urea/ammonia spirit;
Second step: remove the solution of carrying secretly in the flue gas after one-level absorbs, make again this flue gas with blending the urea liquid of additive carry out gas-liquid and contact, reaction is finished the back and is discharged, the liquid-gas ratio of flue gas is 5～20L/m after above-mentioned urea liquid and the one-level absorption
3The mass concentration of urea in containing the solution of additive is 4%～13%, and the solution that contains additive maintains 5.5～8 as secondary absorbent solution and its pH value, and temperature is controlled at 30 ℃～60 ℃, the addition of additive is 0.005%～0.025% mass percent of urea liquid
Described additive is one or more the mixture in triethanolamine, ethylenediamine, the phosphamide.
2, mixed solution according to claim 1 is united and is removed sulfur dioxide and nitrogen oxide method, it is characterized in that the flue gas after secondary absorbs, and discharges after demister is removed the liquid of carrying secretly in the flue gas.
3, a kind ofly be used to implement the described mixed solution of claim 1 and unite the device that removes sulfur dioxide and nitrogen oxide method, it is characterized in that by heat exchanger (1), one-level gas distributor (2), one-level absorption reactor thermally (3), one-level demister (4), secondary gas distributor (5), secondary absorption reactor thermally (6), secondary demister (7), secondary circulating pump (10), secondary collecting tank (11), pump (12), centrifuge (13), one-level collecting tank (15), separate liquid pump (16), air compressor machine (17), one-level circulating pump (18) is formed, one-level gas distributor (2) is located in the one-level absorption reactor thermally (3), secondary gas distributor (5) is located in the secondary absorption reactor thermally (6), the exhanst gas outlet of heat exchanger (1) is connected with one-level absorption reactor thermally smoke inlet (21), the flue gas gas outlet of one-level absorption reactor thermally (3) is connected with the smoke air inlet of secondary absorption reactor thermally (6), one-level demister (4) is positioned between the smoke air inlet of the flue gas gas outlet of one-level absorption reactor thermally (3) and secondary absorption reactor thermally (6), secondary demister (7) is located on the secondary absorption reactor thermally exhanst gas outlet (25), one-level collecting tank (15) is located at the below of one-level absorption reactor thermally (3), between the circulation fluid outlet that one-level circulating pump (18) is located at one-level collecting tank (15) and the inlet of one-level absorption reactor thermally (3) and the import of one-level circulating pump (18) be connected with the circulation fluid outlet of one-level collecting tank (15), the outlet of one-level circulating pump (18) is connected with the inlet of one-level absorption reactor thermally (3), secondary collecting tank (11) is located at the below of secondary absorption reactor thermally (6), between the circulation fluid outlet that secondary circulating pump (10) is located at secondary collecting tank (11) and the inlet of secondary absorption reactor thermally (6) and the import of secondary circulating pump (10) be connected with secondary collecting tank (11) circulation fluid outlet, the outlet of secondary circulating pump (10) is connected with the inlet of secondary absorption reactor thermally (6), the ammonium sulfate crystallization solution outlet of one-level collecting tank (15) is connected with the import of centrifuge (13), the liquid outlet of centrifuge (13) with separate liquid pump (16) import and be connected, separating liquid pump (16) outlet is connected with the import of one-level collecting tank (15), the outlet of air compressor machine (17) is connected with the import of one-level collecting tank (15), and the dense ammonium sulfite solution outlet of secondary collecting tank (11) is connected with the import of one-level collecting tank (15) by pump (12).
4, device according to claim 3, it is characterized in that the import that is connected with aqua ammonia pump (19) and one-level collecting tank (15) in the import of one-level collecting tank (15) is connected with the outlet of aqua ammonia pump (19), the import that is connected with ammoniacal liquor Agitation Tank (20) and aqua ammonia pump (19) on aqua ammonia pump (19) is connected with the outlet of ammoniacal liquor Agitation Tank (20).
5, according to claim 3 or 4 described devices, it is characterized in that the import that is connected with urea solution pump (8) and one-level collecting tank (15) in the import of one-level collecting tank (15) is connected with the outlet of urea solution pump (8), the import that is connected with urea liquid Agitation Tank (9) and urea solution pump (8) on urea solution pump (8) is connected with the outlet of urea liquid Agitation Tank (9).
6, device according to claim 3 is characterized in that being provided with valve (14) between the import of the ammonium sulfate crystallization solution outlet of one-level collecting tank (15) and centrifuge (13).
7, device according to claim 3, it is characterized in that the purification of secondary absorption reactor thermally exhanst gas outlet (25) and heat exchanger (1) after the low-temperature flue gas import be connected.
8, a kind ofly be used to implement the described mixed solution of claim 1 and unite the device that removes sulfur dioxide and nitrogen oxide method, it is characterized in that by heat exchanger (1), monoblock type one second reactor, secondary demister (7), secondary circulating pump (10), pump (12), centrifuge (13), separate liquid pump (16), air compressor machine (17), one-level circulating pump (18) is formed, monoblock type one second reactor comprises cylindrical shell (28), a space that is provided with dividing plate (23) and is surrounded by this dividing plate (23) and cylindrical shell (28) in cylindrical shell (28) is one-level absorption reactor thermally (3), another space that is surrounded by this dividing plate (23) and cylindrical shell (28) is secondary absorption reactor thermally (6), on one-level absorption reactor thermally (3), be provided with one-level absorption reactor thermally smoke inlet (21), be provided with one-level gas distributor (2) in the bottom of one-level absorption reactor thermally (3), be connected with one-level collecting tank (15) in the lower end of one-level absorption reactor thermally (3), be provided with one-level demister (4) on the top of one-level absorption reactor thermally (3), in one-level absorption reactor thermally (3) and the below that is positioned at one-level demister (4) be provided with one-level spray thrower (22), and the nozzle of one-level spray thrower (22) is downward, on secondary absorption reactor thermally (6), be provided with secondary absorption reactor thermally exhanst gas outlet (25), be connected with secondary collecting tank (11) in the lower end of secondary absorption reactor thermally (6), be provided with secondary gas distributor (5) on the top of secondary absorption reactor thermally (6), in secondary absorption reactor thermally (6) and be positioned at secondary gas distributor (5) below to be provided with the nozzle of secondary spray thrower (24) and secondary spray thrower (24) downward, one-level demister (4) and secondary gas distributor (5) are by channel connection, the exhanst gas outlet of above-mentioned heat exchanger (1) is connected with one-level absorption reactor thermally smoke inlet (21), secondary demister (7) is located on the secondary absorption reactor thermally exhanst gas outlet (25), between the circulation fluid outlet that one-level circulating pump (18) is located at one-level collecting tank (15) and the inlet of one-level spray thrower (22) and the import of one-level circulating pump (18) be connected with the circulation fluid outlet of one-level collecting tank (15), the outlet of one-level circulating pump (18) is connected with the inlet of one-level spray thrower (22), between the circulation fluid outlet that secondary circulating pump (10) is located at secondary collecting tank (11) and the inlet of secondary spray thrower (24) and the import of secondary circulating pump (10) be connected with secondary collecting tank (11) circulation fluid outlet, the outlet of secondary circulating pump (10) is connected with the inlet of secondary spray thrower (24), the outlet of secondary circulating pump (10) is connected with the inlet of secondary absorption reactor thermally (6), the ammonium sulfate crystallization solution outlet of one-level collecting tank (15) is connected with the import of centrifuge (13), the liquid outlet of centrifuge (13) with separate liquid pump (16) import and be connected, separating liquid pump (16) outlet is connected with the import of one-level collecting tank (15), the outlet of air compressor machine (17) is connected with the import of one-level collecting tank (15), and the dense ammonium sulfite solution outlet of secondary collecting tank (11) is connected with the import of one-level collecting tank (15) by pump (12).
9, a kind ofly be used to implement the described mixed solution of claim 1 and unite the device that removes sulfur dioxide and nitrogen oxide method, it is characterized in that by heat exchanger (1), monoblock type one second reactor, secondary demister (7), secondary circulating pump (10), pump (12), centrifuge (13), separate liquid pump (16), air compressor machine (17), one-level circulating pump (18) is formed, monoblock type one second reactor comprises cylindrical shell (28), a space that is provided with dividing plate (23) and is surrounded by this dividing plate (23) and cylindrical shell (28) in cylindrical shell (28) is one-level absorption reactor thermally (3), another space that is surrounded by this dividing plate (23) and cylindrical shell (28) is secondary absorption reactor thermally (6), on one-level absorption reactor thermally (3), be provided with one-level absorption reactor thermally smoke inlet (21), be provided with one-level gas distributor (2) in the bottom of one-level absorption reactor thermally (3), be connected with one-level collecting tank (15) in the lower end of one-level absorption reactor thermally (3), be provided with one-level demister (4) on the top of one-level absorption reactor thermally (3), be provided with one-level fluid column formula injector (26) in one-level absorption reactor thermally (3) bottom and above being positioned at one-level gas distributor (2), and the nozzle of one-level fluid column formula injector (26) upwards, on secondary absorption reactor thermally (6), be provided with secondary absorption reactor thermally exhanst gas outlet (25), be connected with secondary collecting tank (11) in the lower end of secondary absorption reactor thermally (6), be provided with secondary gas distributor (5) on the top of secondary absorption reactor thermally (6), the nozzle that is provided with secondary fluid column formula injector (27) and secondary fluid column formula injector (27) in the bottom of secondary absorption reactor thermally (6) makes progress, one-level demister (4) and secondary gas distributor (5) are by channel connection, the exhanst gas outlet of above-mentioned heat exchanger (1) is connected with one-level absorption reactor thermally smoke inlet (21), secondary demister (7) is located on the secondary absorption reactor thermally exhanst gas outlet (25), between the circulation fluid outlet that one-level circulating pump (18) is located at one-level collecting tank (15) and the inlet of one-level fluid column formula injector (26) and the import of one-level circulating pump (18) be connected with the circulation fluid outlet of one-level collecting tank (15), the outlet of one-level circulating pump (18) is connected with the inlet of one-level fluid column formula injector (26), between the circulation fluid outlet that secondary circulating pump (10) is located at secondary collecting tank (11) and the inlet of secondary fluid column formula injector (27) and the import of secondary circulating pump (10) be connected with secondary collecting tank (11) circulation fluid outlet, the outlet of secondary circulating pump (10) is connected with the inlet of secondary fluid column formula injector (27), the outlet of secondary circulating pump (10) is connected with the inlet of secondary absorption reactor thermally (6), the ammonium sulfate crystallization solution outlet of one-level collecting tank (15) is connected with the import of centrifuge (13), the liquid outlet of centrifuge (13) with separate liquid pump (16) import and be connected, separating liquid pump (16) outlet is connected with the import of one-level collecting tank (15), the outlet of air compressor machine (17) is connected with the import of one-level collecting tank (15), and the dense ammonium sulfite solution outlet of secondary collecting tank (11) is connected with the import of one-level collecting tank (15) by pump (12).
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| CN102188897B (en) * | 2011-05-11 | 2013-03-13 | 国电科学技术研究院 | Wet flue gas desulfurization and denitrification combined method |
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