CN213761252U - Flue gas SO2Desorption acid-making cooperative working system - Google Patents
Flue gas SO2Desorption acid-making cooperative working system Download PDFInfo
- Publication number
- CN213761252U CN213761252U CN202022740196.1U CN202022740196U CN213761252U CN 213761252 U CN213761252 U CN 213761252U CN 202022740196 U CN202022740196 U CN 202022740196U CN 213761252 U CN213761252 U CN 213761252U
- Authority
- CN
- China
- Prior art keywords
- channel
- desorption
- flue gas
- acid
- steam
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model provides a flue gas SO2Desorption system acid collaborative work system that desorption includes: desulfurizing tower, rich liquid heater, gas stripping desorption tower, lean liquid cooler, cavitation desorption system, sulfate radical neutralization system, condensing system and sulfurAn acid production system and a condensate oxidizer. The utility model takes the alkaline aluminum sulfate as the desulfurizer to remove the SO in the flue gas2The technologies of desorption, acid making and the like are organically combined, and the problem of flue gas SO is systematically solved2A plurality of mutual balance problems related to desorption, acid making are caused to lead SO2The removal, desorption and acid making process flow work cooperatively to produce sulfuric acid products, SO that the flue gas SO is realized2And (5) recycling.
Description
Technical Field
The utility model belongs to environmental engineering and abandonmentThe technical field of material recycling, in particular to flue gas SO taking alkaline aluminum sulfate as a desulfurizer2Desorption acid preparation cooperative work system.
Background
The basic aluminium sulfate desorption desulfurization method is theoretically one of SO removal and desorption2High efficiency, desorption of SO from the desulfurized rich solution2The post-regenerated basic aluminum sulfate is recycled, and the product SO is desorbed2Can produce sulfuric acid for sale, and has double values of sulfur dioxide pollution treatment and coal sulfur resource.
The existing basic aluminum sulfate desulfuration, desulfuration pregnant solution desorption and desorption products SO2The three technologies for producing sulfuric acid by gas have the problems of mutual balance of a plurality of parameters, most of the technologies lack organic connection or are limited to two connected technologies, and lack of flue gas SO2The removal, desorption and acid making cooperative work system and method enable the alkaline aluminum sulfate wet flue gas desulfurization, desorption and acid making technology to be in SO2The coal-fired flue gas with lower concentration can not be applied.
The previously disclosed method of recycling nitrogen in a desorber, although integrated with an acid making process, does not provide SO2Desorption for preparing acid and SO2Removal of cooperative working system, unresolved SO2The problems of mutual balance involved in removal, desorption and acid preparation are not adopted in the engineering practice.
Flue gas SO with alkaline aluminum sulfate as desulfurizer2The removal, desorption and acid preparation are complex system engineering and need to comprehensively and systematically solve the problem of SO2The removal, desorption and acid preparation relate to a plurality of mutual balance control problems. Especially the temperature control of each circulation of the desulfurization liquid, the oxidation inhibition of sulfite, the standard reaching of desulfurization efficiency and the cost control, and the desorption to obtain SO2Gas is controlled according to the concentration requirement of acid making, SO2Cost control of desorption and acid production, SO2The key problems of improving the desorption rate, the desorption efficiency, the regeneration rate of the desulfurizer and the like need to be cooperatively solved.
SUMMERY OF THE UTILITY MODEL
The purpose of the utility model is to ensure that the basic aluminum sulfate solution is the same as SO2The reversible reaction characteristic related to the temperature provides a flue gas SO2A synergistic working system for desorption acid production, which takes alkaline aluminum sulfate as a desulfurizer to remove SO in the flue gas2The technologies of desorption, acid making and the like are organically combined, systematically coordinated and solved for the SO in the flue gas2The removal, desorption and acid preparation relate to a plurality of mutual balance control problems.
In order to achieve the above object, the utility model provides a following scheme: the utility model provides a flue gas SO2Desorption system acid preparation collaborative work system that desorption, its characterized in that includes: the system comprises a desulfurizing tower, a rich liquid heater, a gas stripping desorption tower, a lean liquid cooler, a cavitation desorption system, a sulfate radical neutralization system, a condensing system, a sulfuric acid manufacturing system and a condensed water oxidizer;
the desulfurizing tower is connected with the rich liquid heater through a cooling flue gas channel and a first rich liquid channel, and the desulfurizing tower is connected with the cavitation desorption system through a second rich liquid channel;
the rich liquid heater is connected with the stripping desorption tower through a third rich liquid channel; the rich liquid heater is also connected with a heat source channel;
the gas stripping desorption tower is connected with the lean liquid cooler through a second lean liquid channel and is connected with the sulfate radical neutralization system through a lean liquid bypass channel; the gas stripping desorption tower is also connected with the condensing system through a first exhaust channel;
the barren liquor cooler is connected with the desulfurizing tower through a first barren liquor channel;
the cavitation desorption system is connected with the sulfate radical neutralization system through a third barren solution channel and is connected with the condensation system through a second exhaust channel;
the sulfate radical neutralization system is connected with the desulfurizing tower through a neutralization regeneration liquid channel;
the condensing system is connected with the sulfuric acid manufacturing system through a third exhaust channel and is connected with the condensed water oxidizer through a fourth condensed water channel; the condensing system is also connected with the cavitation desorption system through a second condensed water channel;
the sulfuric acid manufacturing system is connected with the cavitation desorption system through a third steam channel and is connected with the rich liquid heater or the desulfurizing tower through a second tail gas channel; the sulfuric acid manufacturing system is also connected with the gas stripping desorption tower through a first tail gas channel;
the condensate oxidizer is connected to the sulfuric acid production system through an absorption acid dilution water passage.
Preferably, the heat source channel comprises a raw flue gas channel.
Preferably, the raw flue gas channel can also be connected with the desulfurization tower.
Preferably, the heat source passage further includes a first steam passage and a first condensed water passage.
Preferably, the desulfurizing tower is also connected with a rich liquid recycling channel and a purified flue gas channel;
the rich liquid recycling channel can convey the desulfurization rich liquid at the bottom of the desulfurization tower to the top for cyclic desulfurization;
the purified flue gas channel is used for discharging purified flue gas generated by the desulfurizing tower.
Preferably, the cavitation desorption system is also connected with a second steam channel and a third condensed water channel;
the second steam channel is used for conveying steam extracted by a steam turbine or exhausted steam or water steam of other steam sources;
and the third condensed water channel is used for sending the steam condensed water of the cavitation desorption system to the water steam heat source regenerative system.
Preferably, the sulfate neutralization system is also connected with a feed channel and a gypsum channel;
the feed channel is used for conveying a neutralization raw material to the sulfate radical neutralization system and maintaining the water quantity balance and the aluminum quantity balance of the system;
the gypsum channel is used for discharging the calcium sulfate generated by the sulfate radical neutralization system and the smoke dust captured by the desulfurization solution.
Preferably, the sulfuric acid production system is further connected with a first air channel and a product acid channel;
the first air channel is used for conveying air or oxygen to the sulfuric acid manufacturing system;
the product acid passage is used for conveying sulfuric acid produced by the sulfuric acid production system.
Preferably, the condensed water oxidizer is further connected with a second air channel and an exhaust gas channel;
the second air channel is used for introducing air or oxygen into the condensed water oxidizer;
the waste gas channel is used for discharging waste gas in the condensed water oxidizer.
The utility model discloses a following technological effect:
(1) the utility model utilizes the basic aluminum sulfate and SO2Temperature dependent reversible reaction characteristics of flue gas SO2The technologies of desorption, sulfuric acid production, waste heat utilization, water vapor condensation and the like are organically combined to form the flue gas SO2The system for removing desorption acid preparation cooperative work systematically coordinates and solves the problem of SO in the flue gas2The removal, desorption and acid preparation relate to a plurality of mutual balance problems, and the cooperative working effect of the related process flow is fully exerted. The flue gas purification reaches the standard and is discharged, the desulfurizer is recycled, the desulfurization cost is obviously reduced, and the desulfurization rich solution SO2The heat consumption and the cost of desorption are obviously reduced, and the acid gas SO is obtained by desorption2The concentration is convenient to adjust and control, the industrial waste heat is effectively utilized, and SO in the flue gas2The goal of efficient conversion to a market-competitive sulfuric acid product is achieved;
(2) the utility model adopts SO2The gas stripping and cavitation desorption technology are combined to make the rich liquid desulfurized each time desorbed as much as possible in time, limit the gas ratio of the desulfurized liquid and prepare acid SO2Oxygen deficiency conversion and acid making tail gas SO2The measures such as re-purification in a desulfurizing tower and the like inhibit the sulfite oxidation rate in the desulfurizing-desorbing process flow, reduce the calcium carbonate consumption, improve the sulfuric acid yield, and reduce the gypsum discharge and the aluminum content loss of system liquid;
(3) the utility model can utilize the residual heat of the flue gas when the rich desulfurization solution is heated by the flue gas,but also can reduce the temperature of the flue gas entering the desulfurizing tower, and has double meanings of saving energy and reducing the investment of regenerated liquid cooling equipment sent into the desulfurizing tower. On the occasion that the desulfurization rich solution is not suitable for flue gas heating, the latent heat of industrial dead steam is used as a heating and cavitation desorption heat source of the desulfurization rich solution, SO that SO is obviously reduced2And (4) desorption cost. The wet cooling and air cooling technology can be adopted to cool the desorption barren solution and condense the water vapor of the mixed gas obtained by desorption, and the method is suitable for both water-rich areas and water-deficient areas;
(4) the utility model discloses a limestone/gypsum wet flue gas desulfurization system that has moved, through shutting down existing desulfurizing tower oxidation system, the desulfurization liquid business turn over pipeline installs additional switching bypass can become to use alkaline aluminum sulfate solution as the desulfurizing tower of desulfurization liquid, adopts former limestone slurry preparation and the gypsum desorption system about 10% working capacity can satisfy the utility model discloses sulfate radical neutralization system task requirement, adopt former system water treatment facilities can satisfy the desulfurization liquid pollution treatment requirement, still can conveniently switch to former desulfurization method operation when necessary;
(5) the SO of the utility model2The desorption and acid-making equipment can be arranged close to the desulfurization device or arranged in the open space around the desulfurization tower, and the desorption and acid-making equipment and the desulfurization device are connected by necessary gas (steam) and liquid channels, so that the desorption and acid-making equipment has no special requirements on the layout space and is suitable for new construction or modification of the existing desulfurization system.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without inventive labor.
FIG. 1 shows flue gas SO of a first embodiment of the present invention2The structure schematic diagram of the desorption acid-making cooperative work system is as follows: 1. a desulfurizing tower; 2. a rich liquid heater; 3. a gas stripping desorption tower; 4. a lean liquid cooler; 5. a cavitation desorption system; 6. a sulfate radical neutralization system; 7. a condensing system; 8. a sulfuric acid production system; 9. coagulation of waterA water-forming oxidizer; 10. a cooling flue gas channel; 11. a raw flue gas channel; 12. a second exhaust gas channel; 13. a first lean liquid passage; 14. a neutralizing regeneration liquid channel; 15. a flue gas purification channel; 16. a first rich liquid channel; 17. a second rich liquid channel; 18. a rich liquid recirculation passage; 19. a third rich liquid channel; 22. a first exhaust gas channel; 23. a second lean liquid passage; 24. a first exhaust passage; 25. a lean liquid bypass channel; 26. a second condensed water passage; 27. a second steam channel; 28. a third steam passage; 29. a third lean liquid passage; 30. a second exhaust passage; 31. a third condensed water passage; 32. a feed channel; 33. a gypsum channel; 34. a third exhaust passage; 35. a fourth condensed water passage; 36. a first air passage; 37. an absorption acid dilution water channel; 38. a product acid channel; 39. a second air passage; 40. an exhaust gas passage;
FIG. 2 shows a flue gas SO according to a second embodiment of the present invention2The structure schematic diagram of the desorption acid-making cooperative work system is as follows: 20. a first steam passage; 21. a first condensate passage.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Example 1
As shown in FIG. 1, the embodiment provides the flue gas SO with the flue gas as the heat source of the rich liquid heater2The desorption acid-making cooperative work system comprises a desulfurizing tower 1, a rich liquid heater 2, a gas stripping desorption tower 3, a lean liquid cooler 4, a cavitation desorption system 5, a sulfate radical neutralization system 6, a condensing system 7, a sulfuric acid manufacturing system 8 and a condensed water oxidizer 9;
the desulfurizing tower 1 and the rich liquid heater 2 are mutually connected through a cooling flue gas channel 10 and a first rich liquid channel 16, and the desulfurizing tower 1 is connected with the cavitation desorption system 5 through a second rich liquid channel 17; the desulfurizing tower 1 is also provided with a rich liquid recycling channel 18 which can convey the desulfurizing rich liquid at the bottom of the desulfurizing tower 1 to the top for cyclic desulfurization; the desulfurizing tower 1 is also connected with a purified flue gas channel 15, and the purified flue gas channel 15 can discharge the purified flue gas generated by the desulfurizing tower 1;
the rich liquid heater 2 is connected with the stripping desorption tower 3 through a third rich liquid channel 19; the rich liquor heater 2 is also connected with a raw flue gas channel 11, and the raw flue gas channel 11 can receive raw flue gas from a dust remover;
the stripping desorption tower 3 is connected with the lean liquid cooler 4 through a second lean liquid channel 23 and is connected with the sulfate radical neutralization system 6 through a lean liquid bypass channel 25; the gas stripping desorption tower 3 is also connected with a condensing system 7 through a first exhaust passage 24;
the lean liquid cooler 4 is connected with the desulfurizing tower 1 through a first lean liquid channel 13;
the cavitation desorption system 5 is connected with the sulfate radical neutralization system 6 through a third barren solution channel 29 and is connected with the condensation system 7 through a second exhaust channel 30; the cavitation desorption system 5 is also connected with a second steam channel 27 and a third condensed water channel 31, and the second steam channel 27 can convey water vapor to the cavitation desorption system 5; the third condensed water channel 31 can send the steam condensed water in the cavitation desorption system 5 to the water steam heat source regenerative system;
the sulfate radical neutralization system 6 is connected with the desulfurizing tower 1 through a neutralization regeneration liquid channel 14; the sulfate radical neutralization system 6 is also connected with a feed channel 32 and a gypsum channel 33, and the sulfate radicals in the sulfate radical neutralization system 6 are removed by adding limestone powder or slurry into the feed channel 32, wherein the removal quantity is balanced with the quantity of sulfate radicals oxidized into sulfate radicals in the desulfurization-desorption process flow; the gypsum channel 33 is used for discharging calcium sulfate generated by the sulfate radical neutralization system 6 during the neutralization process and desulfurization liquid capture smoke;
the condensing system 7 is connected with the sulfuric acid production system 8 through a third exhaust passage 34 and is connected with the condensed water oxidizer 9 through a fourth condensed water passage 35; the condensing system 7 is also connected with the cavitation desorption system 5 through a second condensed water channel 26;
the sulfuric acid manufacturing system 8 is connected with the cavitation desorption system 5 through a third steam channel 28 and is connected with the rich liquid heater 2 through a second tail gas channel 12, and the sulfuric acid manufacturing system 8 is also connected with the gas stripping desorption tower 3 through a first tail gas channel 22; the sulfuric acid manufacturing system 8 is also connected with a first air channel 36 and a product acid channel 38, and the first air channel 36 can convey air or oxygen into the sulfuric acid manufacturing system 8; the product acid channel 38 is capable of outputting sulfuric acid produced by the sulfuric acid production system 8;
the condensed water oxidizer 9 is connected to the sulfuric acid production system 8 through an absorption acid dilution water passage 37; the condensed water oxidizer 9 is also connected with a second air channel 39 and an exhaust gas channel 40, and the second air channel 39 can convey air or oxygen into the condensed water oxidizer 9; the exhaust gas passage 40 can exhaust the exhaust gas generated by the condensed water oxidizer 9.
The utility model discloses a flue gas SO that the flue gas is rich liquid heater heat source2The working process of the desorption acid preparation cooperative working system is as follows:
mixing the cooled lean solution sent from the first lean solution channel 13 and the neutralized regenerated solution sent from the neutralized regenerated solution channel 14 at the inlet of a spraying system of the desulfurizing tower 1 to obtain a desulfurized liquid with the temperature of not more than 50 ℃; the desulfurization liquid is sent into a spraying system of a desulfurization tower 1 for spraying and is in reverse flow contact with the original flue gas and the tail gas of acid making for SO, wherein the original flue gas is subjected to heat exchange and temperature reduction by a rich liquid heater 22And removing to obtain purified flue gas and a desulfurization rich solution, and discharging the purified flue gas through a purified flue gas channel 15.
In the embodiment, the temperature of the desulfurization liquid, namely the cooling barren solution and the neutralization regeneration liquid, entering the inlet of the spray system of the desulfurization tower 1 is controlled below 50 ℃, the alkalinity can be 5-50%, the aluminum content can be more than 5g/L, and the desulfurization liquid is combined with the flue gas SO2Parameters such as concentration, desulfurization liquid-gas ratio, liquid temperature and the like are optimally selected, and the oxidation rate of sulfite is reduced as much as possible on the premise of meeting the emission standard of purified flue gas; the temperature of the liquid entering the spray system of the desulfurizing tower 1 is mainly realized by adjusting the working condition of the barren solution cooler 4.
Part of the desulfurization rich liquid in the desulfurization tower 1 is conveyed to the rich liquid heater 2 through the first rich liquid channel 16; the rich liquid heater 2 exchanges heat between the desulfurization rich liquid and high-temperature raw flue gas of the dust remover input from the raw flue gas channel 11 and high-temperature acid making tail gas input from the second tail gas channel 12, the desulfurization rich liquid is heated to a temperature higher than 53 ℃, the raw flue gas and the acid making tail gas are cooled to obtain low-temperature raw flue gas and acid making tail gas, and the low-temperature raw flue gas and the acid making tail gas are conveyed into the desulfurizing tower 1 through the cooling flue gas channel 10.
Delivering the desulfurization rich solution heated by the rich solution heater 2 to a gas stripping desorption tower 3 through a third rich solution channel 19 for gas stripping desorption to obtain a product containing nitrogen, water vapor and SO2The mixed gas and the desulfurization barren solution; the desulfurized lean liquid is sent to the lean liquid cooler 4 through the second lean liquid passage 23 to be cooled to less than 49 ℃, and is input as a desulfurized liquid to the desulfurizing tower 1 through the first lean liquid passage 13 to be subjected to a desulfurization cycle.
Part of the desulfurization rich solution in the desulfurization tower 1 is conveyed to a cavitation desorption system 5 through a second rich solution channel 17 for cavitation desorption to obtain the desulfurization lean solution and the desulfurization lean solution containing water vapor and SO2The mixed gas of (3); the desulfurized lean solution is delivered to the sulfate radical neutralization system 6 through the third lean solution channel 29 for deep regeneration, and the neutralized regenerated solution is obtained and is input to the desulfurizing tower 1 through the neutralized regenerated solution channel 14 as the desulfurized liquid for circulating desulfurization.
The specific working process of the cavitation desorption system 5 in this embodiment is as follows:
distributing the desulfurization rich solution into a labyrinth cavitation desorption chamber through a desorption solution inlet header of the cavitation desorption system 5, so that the desulfurization rich solution is submerged in a cavitation-condensation interface to a set depth; SO supplied from the third steam passage 282Steam produced by oxidation heat and steam extracted or exhausted by a steam turbine sent by a second steam channel 27 are sent to a labyrinth steam heating chamber for heating a cavitation-condensing interface; the desulfurization rich liquid entering the labyrinth cavitation desorption chamber absorbs a large amount of heat from the end part and the side surface of the desulfurization rich liquid to be desorbed in the wave groove to generate violent cavitation in the process of flowing from the liquid inlet end to the liquid outlet end of the wave groove in the cavitation desorption chamber, SO that SO is generated under the synergistic action of cavitation and gas stripping2Quick desorption, regeneration of basic aluminium sulfate to obtain desulfurized barren solution and desorbed SO2Mixing the gas with water vapor;the desulfurization rich solution in the wave groove of the labyrinth cavitation desorption chamber generates cavitation to absorb heat, so that the water vapor in the labyrinth vapor heating chamber forms condensed water on the lower surface of the wave groove, the condensed water is collected at the bottom of the heating chamber, and the condensed water is sent back to a heat regeneration system of a related vapor source through a third condensed water channel 31.
The specific working process of the sulfate radical neutralization system 6 in the embodiment is as follows:
desorbing the cavitation desorption system 5 to obtain desulfurization barren solution, conveying the desulfurization barren solution to a sulfate radical neutralization system 6 through a third barren solution channel 29, adding limestone powder or slurry through a feeding channel 32 to remove sulfate radicals in the desulfurization barren solution to generate calcium sulfate, wherein the removal amount is balanced with the amount of sulfate radicals oxidized into sulfate radicals in the desulfurization-desorption process flow; the calcium sulfate and the desulphurization solution generated by the gypsum channel 33 capture the smoke dust and discharge the smoke dust outside the system of the utility model.
The aluminum carried by the gypsum is removed, the aluminum sulfate is supplied through the feed channel 32 to keep the balance of the aluminum content of the alkaline aluminum sulfate solution in the system, and the water is supplied through the feed channel 32 to wash the gypsum to reduce the aluminum carried by the gypsum and keep the balance of the water content in the system.
The sulfate neutralization system 6 can also directly and deeply regenerate the removal of sulfate from the desulfurization lean solution in the stripping and desorption tower 3 through the lean solution bypass passage 25.
Desorbing the stripping desorption tower 3 and the cavitation desorption system 5 to obtain the product containing nitrogen, water vapor and SO2The mixed gas is respectively conveyed to the condensing system 7 through the first exhaust channel 24 and the second exhaust channel 30 for condensation, and the water vapor is converted into condensate water rich in sulfite so as to remove the water vapor in the mixed gas; the condensed water is respectively conveyed to the cavitation desorption system 5 and the condensed water oxidizer 9 through the second condensed water channel 26 and the fourth condensed water channel 35, and is respectively subjected to re-desorption or oxidation conversion; the condensed water can also be sent into the gas stripping desorption tower 3 for desorption through a connecting channel.
Blowing air or oxygen into the condensed water oxidizer 9 through the second air passage 39 to oxidize and convert the condensed water in the condensed water oxidizer 9 to form the acid-absorbed dilution water required for sulfuric acid production, and passing the acid-absorbed dilution waterThe channel 37 is sent to the sulfuric acid manufacturing system 8 for use; the exhaust gas from the condensate oxidizer 9 is discharged through an exhaust gas passage 40, if containing SO2The gas is sent to the desulfurizing tower 1 to be purified and discharged.
The mixed gas after the water vapor is removed by the condensing system 7 is conveyed to the sulfuric acid manufacturing system 8 through the third exhaust passage 34, and is mixed with the air or the oxygen sent by the first air passage 36 to form SO2The concentration of the acid-making fresh gas meets the technological requirements of sulfuric acid production, and the acid-making fresh gas is dried and SO2Oxidation to SO3And SO3Absorption and other technological processes to obtain sulfuric acid with set concentration and acid making tail gas, outputting the generated sulfuric acid through a product acid channel 38, and conveying the acid making tail gas required by gas stripping desorption to a gas stripping desorption tower 3 through a first tail gas channel 22 according to required amount to desorb SO2Meanwhile, the residual acid making tail gas is conveyed to the desulfurizing tower 1 through the second tail gas channel 12 to be purified and discharged.
SO contained in the desorbed gas supplied to the sulfuric acid production system 8 after mixing with air2The concentration is determined by the requirements of the sulfuric acid production process, and the solution is solved by adjusting and controlling the ratio of the desulfurization rich solution fed into the rich solution heater 2 and the cavitation desorption system 5, adjusting the flow of the acid making tail gas fed into the gas stripping desorption tower 3 and adjusting and controlling the amount of air fed into the sulfuric acid manufacturing system 8.
To avoid stripping SO2In the process flow, the oxygen content of sulfite radical oxidation and acid making tail gas is controlled by a standard close to zero, and the oxygen content of input air is preferably less than SO2Oxidation to SO3The theoretical requirement, if necessary, can be reduced appropriately to reduce SO of acid production2Conversion rate index, increase of oxidation catalyst quantity and quality improvement are cooperatively solved, and acid production tail gas SO2The standard exceeding can be purified and reach the standard through the desulfurizing tower 1, and a tail gas desulfurizing device can be additionally arranged for purifying and discharging after reaching the standard.
Example 2
As shown in FIG. 2, the present embodiment provides a method for transforming a limestone/gypsum wet flue gas desulfurization system into a flue gas SO using alkaline aluminum sulfate as a desulfurizing agent and steam as a heat source of a rich liquor heater2A co-operating system for desorption acid production, whereinThe rich liquid heater 2 adopts steam extraction or steam exhaust of a steam turbine as a heating heat source and is connected with a first steam channel 20 and a first condensed water channel 21;
the raw flue gas channel 11 and the second tail gas channel 12 are directly connected with the desulfurizing tower 1, and the raw flue gas and part of acid-making tail gas of the sulfuric acid manufacturing system 8 are directly input into the desulfurizing tower 1 through the raw flue gas channel 11 and the second tail gas channel 12;
the rich liquid heater 2 receives steam turbine exhaust or extraction steam to exchange heat with the desulfurization rich liquid through a first steam channel 20, and sends the condensed water back to the steam source regenerative system through a first condensed water channel 21.
The flue gas described in the embodiment is SO-containing2Such as coal-fired flue gas, smelting furnace tail gas and acid-making tail gas.
The above-mentioned embodiments are only intended to describe the preferred embodiments of the present invention, but not to limit the scope of the present invention, and those skilled in the art should also be able to make various modifications and improvements to the technical solution of the present invention without departing from the spirit of the present invention, and all such modifications and improvements are intended to fall within the scope of the present invention as defined in the appended claims.
Claims (9)
1. Flue gas SO2Desorption system acid preparation collaborative work system that desorption, its characterized in that includes: the system comprises a desulfurizing tower (1), a rich liquid heater (2), a gas stripping desorption tower (3), a lean liquid cooler (4), a cavitation desorption system (5), a sulfate radical neutralization system (6), a condensing system (7), a sulfuric acid manufacturing system (8) and a condensed water oxidizer (9);
the desulfurizing tower (1) and the rich liquid heater (2) are connected with each other through a cooling flue gas channel (10) and a first rich liquid channel (16), and the desulfurizing tower (1) is connected with the cavitation desorption system (5) through a second rich liquid channel (17);
the rich liquid heater (2) is connected with the stripping desorption tower (3) through a third rich liquid channel (19); the rich liquid heater (2) is also connected with a heat source channel;
the stripping desorption tower (3) is connected with the lean liquid cooler (4) through a second lean liquid channel (23) and is connected with the sulfate radical neutralization system (6) through a lean liquid bypass channel (25); the gas stripping desorption tower (3) is also connected with the condensing system (7) through a first exhaust channel (24);
the lean liquid cooler (4) is connected with the desulfurizing tower (1) through a first lean liquid channel (13);
the cavitation desorption system (5) is connected with the sulfate radical neutralization system (6) through a third lean solution channel (29) and is connected with the condensing system (7) through a second exhaust channel (30);
the sulfate radical neutralization system (6) is connected with the desulfurization tower (1) through a neutralization regeneration liquid channel (14);
the condensing system (7) is connected with the sulfuric acid manufacturing system (8) through a third exhaust passage (34) and is connected with the condensed water oxidizer (9) through a fourth condensed water passage (35); the condensing system (7) is also connected with the cavitation desorption system (5) through a second condensed water channel (26);
the sulfuric acid manufacturing system (8) is connected with the cavitation desorption system (5) through a third steam channel (28) and is connected with the rich liquid heater (2) or the desulfurizing tower (1) through a second tail gas channel (12); the sulfuric acid manufacturing system (8) is also connected with the stripping desorption tower (3) through a first tail gas channel (22);
the condensed water oxidizer (9) is connected to the sulfuric acid production system (8) through an absorption acid dilution water passage (37).
2. Flue gas SO according to claim 12The removal and desorption acid preparation cooperative work system is characterized in that the heat source channel comprises a raw flue gas channel (11).
3. Flue gas SO according to claim 22The removal and desorption acid preparation cooperative work system is characterized in that the raw flue gas channel (11) can be also connected with the desulfurizing tower (1).
4. Flue gas SO according to claim 12The desorption and acid preparation cooperative work system is characterized in that the heat source channel also comprises a first steam channel (20) and a second steam channelA condensed water passage (21).
5. Flue gas SO according to claim 12The removal and desorption acid making cooperative work system is characterized in that the desulfurizing tower (1) is also connected with a rich liquid recirculation channel (18) and a flue gas purification channel (15);
the rich liquid recycling channel (18) can convey the desulfurization rich liquid at the bottom of the desulfurization tower (1) to the top for cyclic desulfurization;
the purified flue gas channel (15) is used for discharging the purified flue gas generated by the desulfurizing tower (1).
6. Flue gas SO according to claim 12The desorption and acid preparation cooperative work system is characterized in that the cavitation desorption system (5) is also connected with a second steam channel (27) and a third condensed water channel (31);
the second steam channel (27) is used for conveying steam of extraction steam or exhaust steam of a steam turbine or other steam sources;
the third condensed water channel (31) is used for sending the steam condensed water of the cavitation desorption system (5) to a water steam heat source regenerative system.
7. Flue gas SO according to claim 12The removal and desorption acid preparation cooperative work system is characterized in that the sulfate radical neutralization system (6) is also connected with a feed channel (32) and a gypsum channel (33);
the feed channel (32) is used for conveying a neutralization raw material to the sulfate radical neutralization system (6) and maintaining the water quantity balance and the aluminum quantity balance of the system;
the gypsum channel (33) is used for discharging the calcium sulfate generated by the sulfate radical neutralization system (6) and the smoke captured by the desulfurization solution.
8. Flue gas SO according to claim 12The removal and desorption acid preparation cooperative work system is characterized in that the sulfuric acid manufacturing system (8) is also connected with a first air channel (36) and a product acid channel (38);
the first air channel (36) is used for conveying air or oxygen to the sulfuric acid production system (8);
the product acid channel (38) is used for conveying sulfuric acid produced by the sulfuric acid production system (8).
9. Flue gas SO according to claim 12The desorption acid-making cooperative work system is characterized in that the condensed water oxidizer (9) is also connected with a second air channel (39) and an exhaust gas channel (40);
the second air channel (39) is used for introducing air or oxygen into the condensed water oxidizer (9);
the exhaust gas channel (40) is used for discharging the exhaust gas in the condensed water oxidizer (9).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022740196.1U CN213761252U (en) | 2020-11-24 | 2020-11-24 | Flue gas SO2Desorption acid-making cooperative working system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022740196.1U CN213761252U (en) | 2020-11-24 | 2020-11-24 | Flue gas SO2Desorption acid-making cooperative working system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN213761252U true CN213761252U (en) | 2021-07-23 |
Family
ID=76880472
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022740196.1U Active CN213761252U (en) | 2020-11-24 | 2020-11-24 | Flue gas SO2Desorption acid-making cooperative working system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN213761252U (en) |
-
2020
- 2020-11-24 CN CN202022740196.1U patent/CN213761252U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103303877B (en) | Many sources of the gas low concentration SO 2smoke comprehensive reclaims acid-making process flow process | |
| CN106984169B (en) | Denitration system and method directly utilizing heat of sinter | |
| CN102181308A (en) | Vacuum potassium carbonate coke oven gas desulfurization-sulfuric acid preparation process and processing system thereof | |
| CN103072957A (en) | Technology for preparing sulfuric acid | |
| CN1939840A (en) | Tail gas treatment and reutilization for calcium carbide stove | |
| CN101254392B (en) | Energy-saving type sodium sulphite circulation desulfurizing device and method | |
| CN103977694A (en) | Method and system for removing sulfur dioxide in flue gas | |
| CN104857838A (en) | System and method for flue gas desulfurization through bipolar membrane electrodialysis | |
| CN111847381B (en) | Method and device for preparing hydrogen from industrial waste gas | |
| CN201658945U (en) | Sintering smoke purifying system based on heat pipe afterheat recovery technology | |
| CN104560223B (en) | A kind of gas desulfurizer and method thereof | |
| CN210826085U (en) | Blast furnace gas catalytic desulfurization device | |
| CN113856441B (en) | Ammonia desulfurization method and ammonia desulfurization apparatus | |
| CN105485701A (en) | Coal-fired power generation system deeply and integrally provided with system for desulfurizing and decarburizing calcium-based sorbent in sequence | |
| CN213761252U (en) | Flue gas SO2Desorption acid-making cooperative working system | |
| CN112705000A (en) | Calcium carbide furnace tail gas comprehensive utilization system and process | |
| CN217961993U (en) | Ammonia process desulfurization and decarbonization tower and chemicals coproduction device | |
| CN212523615U (en) | Water-saving and white-removing device for sulfur dioxide in zinc oxide removal flue gas | |
| CN102485325B (en) | Flue gas desulphurization technology with ammonium sulfate-calcium hydroxide slurry method | |
| CN203558850U (en) | Sulfur-containing waste liquid dry method acid making system | |
| CN102876828B (en) | Reducing gas purification process and system matched with gas-based shaft furnace | |
| CN112426871A (en) | Flue gas SO2Desorption and desorption acid preparation cooperative work system and method | |
| CN204973507U (en) | Energy -concerving and environment -protective processing of coking production process flue gas integration system | |
| CN104689702B (en) | High-temperature high-concentration sulfur dioxide tail gas desulfurization system and method | |
| CN111748672B (en) | Short-process low-cost CO preparation method by converter gas2And high-value application system and process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |