CN204891578U - Ammonia - ammonium sulfate method flue gas desulphurization device - Google Patents
Ammonia - ammonium sulfate method flue gas desulphurization device Download PDFInfo
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- CN204891578U CN204891578U CN201520572150.XU CN201520572150U CN204891578U CN 204891578 U CN204891578 U CN 204891578U CN 201520572150 U CN201520572150 U CN 201520572150U CN 204891578 U CN204891578 U CN 204891578U
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Abstract
The utility model discloses an ammonia - ammonium sulfate method flue gas desulphurization device, it includes flue gas desulfurization absorption tower and extrinsic cycle groove, includes oxidation panel, pre -absorption section, extrinsic cycle absorption section, washing section and defogging section in the flue gas desulfurization absorption tower from bottom to top, is equipped with absorption tower cauldron water conservancy diversion bucket in the oxidation panel, absorption tower cauldron water conservancy diversion bucket mainly comprises the straight bucket of lower part and the loudspeaker bucket that upwards enlarges on upper portion, be equipped with the annular sieve that has a plurality of sieve meshes in the pre -absorption section on the floss hole, the outer rampart of annular sieve and the tower wall zonulae occludens of pre -absorption section, the ring baffle that the interior rampart and a vertical direction of annular sieve were set up is connected. The utility model discloses making processes such as flue gas cooling, absorption, oxidation accomplish with an absorption tower, having solved the problem that traditional desulfurization technique flue gas was escaped and is leaded to the absorption efficiency to reduce along the tower wall, oxidation panel and oxidation groove need not mechanical power, and the operation is reliable, reduces plant area and energy consumption.
Description
Technical field
The utility model belongs to environmental technology field, is specifically related to a kind of ammonia ammonium sulphate process flue gas desulfur device.
Background technology
Ammonia type flue gas desulfurizing technology adopts ammonia to remove SO as absorbent
2deng the flue gases purification of pollutant.Early 1970s, Japan to begin one's study ammonia flue gas desulfurization technique technology with the country such as Italy, and in succession obtained successfully, but because the problem such as aerosol in tail gas after the purification of operating cost, burn into, its application receives certain restriction.Enter the nineties in 20th century, along with the reason such as development, technological progress of ammonia synthesizing industry, the application of ammonia type flue gas desulfurizing technology is risen fast.Ammonia type flue gas desulfurizing technology has other feature not available for much flue gas desulfurization technique technique.At present, ammonia is a kind of good alkaline absorbent be easy to get, and from absorption mechanism, alkaline absorbent absorbs the SO in flue gas
2be acid-base neutralization reaction, absorbent alkalescence is stronger, and infiltration rate is faster, and the alkalescence of ammonia is better than calcium-base absorbing agent; And from absorption mechanism, calcium-base absorbing agent absorbs SO
2be gas-solid reaction, reaction speed is slow, and not exclusively, absorbent utilization rate is low in reaction, needs larger energy to carry out absorbing liquid atomization, circulation etc. and improves absorbent utilization rate; And ammonia type flue gas desulfurizing absorption of technology SO
2be gas-liquid or gas-solid/liquid/gas reactions, reaction rate is fast, and absorbent ammonia react is complete, and absorbent utilization rate is high, can accomplish very high desulfuration efficiency, and the process energy consumptions such as absorbing liquid atomization, circulation are low, and equipment volume is little.
Ammonia ammonium sulphate process flue gas desulfurization is a kind of ammonia type flue gas desulfurizing technology, accessory substance is ammonium sulfate, ammonium sulfate can as Fertilizer application in some places, and accessory substance ammonium sulfate takes out the operating cost can offsetting part of smoke desulfurization, and this technology is used widely.In absorption process, formed (NH4)
2sO
3-NH
4hSO
3-H
2the absorbing liquid system of O, NH in this absorbing liquid system
4hSO
3to SO
2not there is absorbability, in this solution (NH4)
2sO
3to SO
2have good absorbability, it is the main absorber in ammonia process.Because of NH in this solution
4hSO
3to SO
2not there is absorbability, so NH in solution
4hSO
3when reaching finite concentration, need process of taking measures, ammonia ammonium sulphate process flue gas desulphurization system, adopt air oxidation and add ammonia controlling measurement absorbent solution in NH
4hSO
3concentration, in absorbent solution, the molar concentration rate of ammonia, ammonium sulfite is reacted by the pH value of solution.So ammonia ammonium sulphate process flue gas desulfurization course absorbing liquid pH value controls extremely important.
Ammonia ammonium sulphate process flue gas desulfurization is a kind of Sulphur ressource reclaiming type technology, and this technology is in Rapid development stage at present, is the study hotspot of coal-fired flue gas desulfurization technology.Reaction principle divides following two steps to carry out: (1) is with the SO in the aqueous solution
2and NH
3reaction based on absorption process, utilize ammonia by the SO in waste gas
2remove, obtain (NH4)
2sO
3-NH
4hSO
3-H
2the absorbing liquid system of O, carry out heat chemistry absorption process:
2NH
4OH+SO
2←→(NH
4)
2SO
3+H
2O(1)
SO
2+(NH
4)
2SO
3+H
2O←→2NH
4HSO
3(2)
NH
4OH+NH
4HSO
3←→(NH
4)
2SO
3+H
2O(3)
There is ionization equilibrium in inferior sulfate radical and bisulfite:
H
++SO
3 2-←→HSO
3 -(4)
(2) adopt air to ammonium sulfite, ammonium bisulfite oxidation, this process is that the intermediate product sulfite oxidation of the instability produced by flue gas desulfurization absorption reaction becomes stable ammonium sulfate.Main oxidation reaction is simply expressed as:
2NH
4HSO
3+O
2→2NH
4HSO
4(1)
2(NH
4)
2SO
3+O
2→2(NH
4)
2SO
4(2)
The absorbing liquid ammonium bisulfite content that ammonia ammonium sulphate process flue gas desulfurization produces is usually far above ammonium sulfite content, so the mainly reaction (1) that the oxidation of ammonia ammonium sulphate process flue gas desulfurization absorbing liquid occurs.Ammonium bisulfite is easily oxidized, and oxidation reaction just can occur at normal temperatures, and temperature raises, and oxidation reaction is accelerated.
Mend ammonia adjust ph, in and acid salt NH
4hSO
4, generate ammonium sulfate:
NH
4HSO
4+NH
4OH→(NH
4)
2SO
4+H
2O(3)
In commercial Application, ammonia ammonium sulphate process technical process is generally: after the flue gas after the dedusting that boiler induced-draft fan (or desulphurization devices) attracts enters desulfurizer, lowers the temperature and react generation (NH4) through ammonia absorbing liquid circulation cleaning
2sO
3-NH
4hSO
3-H
2the absorbing liquid system of O, and ammonium sulfite, bisulfite ammonium salt solution are changed into ammonium sulfate, ammonium bisulfate solution by the air oxygen blasted, mends ammonia adjust ph, in and acid salt NH
4hSO
4, generate ammonium sulfate.Ammonium sulfate self obtains concentrated rear feeding sulphur crystalline ammonium device in washing temperature-fall period.Clean flue gas after desulfurization reaches after environmental protection standard requires through demist and discharges.
The enterprise of foreign study ammonia-process desulfurization technique mainly contains: GE, Marsulex, Pircon, Babcock & Wilcox of the U.S.; Lentjes, Bischoff, KruppKoppers of Germany; NKK, the IHI of Japan, thousand generation field, Sumitomo, Mitsubishi, weak former etc.The Walther ammonia process technique of typical ammonia fume desulphurization method Lu You Ke C Compaq, this technique is that two towers absorb, and equipment is more, and technological process is long, and invest high, energy consumption is high, and plant area area is large; Can Jie Si-than the AMASOX ammonia process technique of little Fu company, this technique main feature is single tower process multitower being transformed into compact conformation, and wet type electrostatic precipitator is installed in tower, the aerosol problem existed in flue gas after solving purification, effectively reduce cost of investment and energy consumption, desulfuration efficiency is high, to flue gas condition change strong adaptability, but this technology is point main absorber portion and time absorber portion in absorption tower, and pressure drop is large, and ammonia consumption is high; The ammonia process technique of GE company, this technique is three tower cascade connected technique, and number of devices is many, and technological process is long, invests high, in flue gas sulfur content comparatively Gao Shicai have superiority.After researching and analysing ammonia ammonium sulphate process flue gas desulfurization technique, we find, current technology respectively has pluses and minuses, also have many can the place of Improvement and perfection, mainly comprise following several aspect:
1) current, in industrial applications, generally adopt cascade towers ammonia ammonium sulphate process technique, compare with single tower process, cascade towers ammonia ammonium sulphate process technique will cool, be oxidized, uptake zone separately, make the electrochemical conditions that each process all keeps best, but still it is long to there is technological process, cost of investment and energy consumption high, the problems such as plant area area is large.
2), in industrial applications, absorber portion is generally adopted not have the void tower of the spray-absorption of internals.In void tower, flue gas can occur along tower wall escape situation, and the desulfuration efficiency of the flue gas of close tower wall is far below the desulfuration efficiency in the middle part of tower.Most of technology does not take measures to process the flue gas along the flowing of tower wall, causes the efficiency of desulfurizing tower low; For addressing this problem, some technology take the method increasing absorbing liquid sprinkle density near tower wall, but absorption process liquid-gas ratio can be caused large, the problem that energy consumption is high.
3) absorption tower oxidation panel is arranged at bottom absorption tower usually, is one of critical section of ammonia ammonium sulphate process flue gas desulfurization.Some technology take the method for oxidation of the direct bubbling of air, and the method air bubble and absorbing liquid do not have good mixing.In order to the air bubble and absorbing liquid that ensure rising have good mixing, some technology are taked to install side agitator, by the stirring acting in conjunction of air bubbling and side agitator, air bubble and absorbing liquid is made to have good mixing, but this method needs machine power, and, side agitator is installed, normal accident absorbing liquid occurring and leaks.Some technology are taked to install outer circulation pump, force outer circulation, utilize machine power that absorbing fluid is circulated at oxidation panel, by the acting in conjunction of air bubbling and absorbing fluid outer circulation, make air bubble and absorbing liquid have good mixing, but this method also need machine power.
4) current, some methods arrange the oxidation trough independent of absorption tower system, and according to oxidation trough pH situation ammoniacal liquor adjust ph.This method generally adopts in the wet fuel gas desulfurizing technologies such as calcium method, sodium method, ammonia process.The major advantage of this method is: 1. can accomplish in oxidation trough, under the electrochemical conditions being different from absorption tower control, complete oxidation, the effective dose of accurate optimization oxidation air, improves the utilization rate of oxygen, lowers operating cost; 2. being convenient to oxidation is the monitoring of running status.Oxidation trough oxidation panel, its version mainly contains following several: directly bubbling mode, installation agitator mode.Direct bubbling mode mixes uneven, and air bubble and absorbing liquid do not have good mixing, and in order to the air bubble and absorbing liquid ensureing rising has good mixing, some methods install agitator in oxidation trough, and this form needs machine power, and energy consumption is high.
Utility model content
The purpose of this utility model is to solve the problem, a kind of ammonia ammonium sulphate process cigarette gas sweetening list tower apparatus of compact conformation is provided, in the utility model on conventional ammonia ammonium sulphate process desulfur technology basis further innovating and developing, in conjunction with the absorbability of ammonia to sulfur dioxide and the advantage of process optimization, the processes such as flue gas cooling, absorption, oxidation are completed with an absorption tower, solve the difficult point that traditional desulfur technology flue gas is escaped along tower wall, oxidation panel and oxidation trough are without the need to machine power, improve oxidation effectiveness, operation is reliable, reduces plant area and energy consumption.
The purpose of this utility model can be reached by following measures:
A kind of ammonia ammonium sulphate process flue gas desulfur device, it comprises fume desulfurating absorption tower and the outer circular slot of hollow, oxidation panel, pre-absorption section, outer circulation absorber portion, washing section and demist section is comprised from bottom to top in described fume desulfurating absorption tower, discharging opening is provided with in the bottom of described oxidation panel, this discharging opening is connected by the entrance of pipeline with lower absorber portion outer circulation pump, and described lower absorber portion outer circulation delivery side of pump is connected with the entrance of absorbing liquid spray equipment in the tower be located in described pre-absorption section by pipeline; Be provided with in described oxidation panel and absorb tower reactor diversing bucket, this absorption tower reactor diversing bucket is formed primarily of the straight bucket of bottom and the loudspeaker bucket upwards expanded on top, be provided with and enter to absorb air sparger in absorption tower reactor diversing bucket that tower reactor oxidation air pipe is connected absorbing the bottom in tower reactor diversing bucket, be provided with in the outside of described absorption tower reactor diversing bucket and absorb tower reactor and mend the absorption tower reactor that ammonia pipe is connected and mend ammonia pipe distributor; Absorbing fluid collector is provided with in described fume desulfurating absorption tower, it is described pre-absorption section between described oxidation panel and absorbing fluid collector, pre-absorption section is connected by floss hole with air inlet flue, annular sieve plate is provided with in pre-absorption section on described floss hole, this annular sieve plate is provided with multiple sieve aperture, the external annulus of annular sieve plate and the tower wall compact siro spinning technology of pre-absorption section, the ring baffle that internal ring wall and a vertical direction of annular sieve plate are set up is connected; The bottom of described absorbing fluid collector is provided with liquid outlet, and the partially liq that this liquid outlet goes outer circulation barrel to be connected absorbing fluid collector is collected with described outer circular slot by absorption tower imports in outer circular slot; The bottom of outer circular slot is provided with circulation fluid outlet, circulation fluid spray equipment is provided with in fume desulfurating absorption tower on described liquid header, described circulation fluid spray equipment to be exported with the circulation fluid of described outer circular slot by pipeline and is connected, and forms described outer circulation absorber portion between described absorbing fluid collector and circulation fluid spray equipment; The water spray system be connected with water inlet pipe is provided with in washing section on described outer circulation absorber portion; Demister is provided with in described demist section.
This method takes multiple technologies means to realize sufficient gas-liquid layout, such as this device can be provided with the absorbing liquid spray equipment that absorbing liquid is contacted with flue gas downstream in air inlet flue, and this absorbing liquid spray equipment is connected with lower absorber portion outer circulation delivery side of pump by removing absorption tower flue absorbing liquid pipe.Utilize the air inlet flue on absorption tower as flue gas cooling zone like this, arrange spraying cooling section in the air inlet flue inside on absorption tower, reduce the temperature of the flue gas into absorption tower on the one hand, the concentrated absorbing liquid decrystallized, saves the energy consumption of crystallization workshop section simultaneously; First the flue gas entering absorption tower uses absorption tower lower liquid cyclic absorption, and absorption tower lower liquid is from oxidation panel, and solution ph controls by adding ammonia, and absorption tower lower liquid controls at acid condition, and the pH value of ie in solution is less than 7.In the utility model, absorption tower lower liquid main component is ammonium sulfate, and assimilation effect is poor.Absorption tower lower liquid had both done flue gas cooling fluid, do again flue gas pre-absorption liquid, and because absorption tower lower liquid also needs to carry out air oxidation process, the sulphite that absorption process is formed constantly is formed, constantly oxidized, so its temperature can top, a little higher than absorption tower absorbing liquid, solution temperature controls at 40 ~ 45 DEG C, is 5.0 ~ 6.3 by the method control ph scope passing into ammonia.
Fume desulfurating absorption tower in this device is hollow structure, and this hollow structure refers to does not have filler and the major part structure that is cavity in tower, but in hollow structure, have the equipment of some necessity yet.Ring baffle in device can utilize the confined space in tower fully, makes gas-liquid contact more abundant.Generally, the edge up and down of ring baffle all exceeds described annular sieve plate, the downflow weir of the top looping sieve plate of this ring baffle, and the bottom of this ring baffle forms flue gas hydraulic barrier.
The fume desulfurating absorption tower of a hollow structure and the independent circulating slot of an outfit of the absorbing fluid on tower top only can be had in this device, carry secretly containing ammonium salt in flue gas after absorption, acid mist etc., wash with water, remove the ammonium salt, acid mist etc. carried secretly, then carry out electric demist.What be provided with to pass into ammonia on the top of outer circular slot enters outer circular slot ammonia pipe.Like this, in the system only having an absorption tower, will cool, be oxidized, uptake zone separately, the electrochemical conditions making each process all keep best, shortens technological process, reduces the problem such as cost of investment and energy consumption.But in a preferred version, this device also can comprise an oxidation trough, described oxidation trough is connected with described lower absorber portion outer circulation delivery side of pump by pipeline; Described oxidation trough is provided with into oxidation trough ammonia pipe; Oxidation trough discharge nozzle is provided with in the bottom of described oxidation trough.From the solution deoxidation groove absorbing tower reactor discharge, add ammonia to oxidation trough and pass into air, the oxidizing process of absorbing fluid can be optimized further.
The utility model employing absorption tower is the spray absorber of tower cornice annular sieve plate, solves flue gas along tower wall escape problem.This device can arrange annular sieve plate structure in pre-absorption section, also can arrange annular sieve plate structure in other parts, particularly all arrange annular sieve plate structure at pre-absorption section, absorber portion and washing section.Such as in described outer circulation absorber portion, be provided with annular sieve plate two, this annular sieve plate two is provided with multiple sieve aperture, the external annulus of annular sieve plate two and the tower wall compact siro spinning technology of outer circulation absorber portion, the ring baffle two that internal ring wall and a vertical direction of annular sieve plate two are set up is connected, the downflow weir of the top looping sieve plate two of this ring baffle two, the bottom of this ring baffle two forms flue gas hydraulic barrier.Further, annular sieve plate three is provided with in described washing section, this annular sieve plate three is provided with multiple sieve aperture, the external annulus of annular sieve plate three and the tower wall compact siro spinning technology of washing section, the ring baffle three that internal ring wall and a vertical direction of annular sieve plate three are set up is connected, the downflow weir of the top looping sieve plate three of this ring baffle three, the bottom of this ring baffle three forms flue gas hydraulic barrier.
The annular sieve plate structure (comprise annular sieve plate, annular sieve plate two, annular sieve plate are third-class) that the utility model adopts is arranged in absorption tower inwall circumferentially, like this in absorption tower, tower central space is the void tower without column plate, is annular sieve plate structure near tower wall.Annular sieve plate end arranges vertically arranged plate (ring baffle, ring baffle two, ring baffle three), and the upper-lower section of plate all exceeds annular sieve plate.Like this, annular sieve plate upper end defines the downflow weir of certain altitude, make on annular sieve plate, form certain thickness absorbing fluid, annular sieve plate lower end just defines flue gas deflection plate, and making rises along tower wall does not flow to direction in the middle part of tower through after the flue gas baffling of annular sieve plate.By this structure, make flue gas that part flows along tower wall by annular sieve plate, part baffling is to the middle part of tower.Like this, when not increasing sprinkle density near tower wall, liquid-gas ratio near tower wall on sieve plate increases, flue gas forms gas-liquid contact through sieve plate, the flue gas risen under annular sieve plate contacts with the liquid also flowed down with sieve plate hole, like this, near tower wall, annular sieve plate upper and lower side absorbs space gas-liquid contact, absorbs space and is utilized effectively.
Annular sieve plate structure in the utility model can be arranged on any one section or several sections in pre-absorption section, outer circulation absorber portion, washing section.After liquid in this device sprays into the fume desulfurating absorption tower of hollow from spray equipment, absorbing liquid spray equipment, circulation fluid spray equipment, absorbing liquid spray equipment place circular treatment in oxidation panel, outer circular slot tower, finally by lower absorber portion outer circulation pump discharge section or whole liquid.Flue gas upwards, carries out counter current absorption with liquid after importing the fume desulfurating absorption tower of hollow from air inlet flue always, and the absorption tower escape pipe finally by tower top is discharged.
The utility model in order to ensure rise air bubble and absorbing liquid have good mixing, improve sub-salt oxidation rate, absorption tower oxidation panel and oxidation trough all adopt the self-loopa of Inner guide bucket, such as in described oxidation trough, be provided with oxidation trough Inner guide bucket, this oxidation trough Inner guide bucket is made up of the straight bucket of bottom and the loudspeaker bucket upwards expanded on top, and the bottom in described oxidation trough Inner guide bucket is provided with and enters air sparger in oxidation trough Inner guide bucket that oxidation trough oxidation air pipe is connected; Be provided with in the outside of described oxidation trough Inner guide bucket with described enter the oxidation trough that is connected of oxidation trough ammonia pipe mend ammonia pipe distributor.Oxidation trough is connected with described lower absorber portion outer circulation delivery side of pump by pipeline; Described oxidation trough is provided with into oxidation trough ammonia pipe; Oxidation trough discharge nozzle is provided with in the bottom of described oxidation trough.
The utility model is by absorption tower oxidation panel and oxidation trough, namely in liquid at the bottom of absorption tower and oxidation trough liquid in install diversing bucket, oxidation air passes in diversing bucket, to cause inside and outside diversing bucket gas holdup difference in liquid, in water conservancy diversion liquid in bucket, gas holdup is high, and in the outer liquid of diversing bucket, gas holdup is low, causes the differential static pressure of fluid, thus produce liquid circulation motion, make absorbing fluid inside and outside diversing bucket between circulation reach diffusion and the object of mass transfer.Because Inner eycle method for oxidation structure is simple, do not need machine power, operation is reliable, decreases electric energy loss.
Air inlet flue in this device passes in pre-absorption section with level or angle obliquely; In air inlet flue, be provided with the absorbing liquid spray equipment that absorbing liquid is contacted with flue gas downstream, this absorbing liquid spray equipment is connected with described lower absorber portion outer circulation delivery side of pump by pipeline.
In this device, be provided with the absorption tower escape pipe that the flue gas after making process discharges fume desulfurating absorption tower at the top of fume desulfurating absorption tower.Pipeline between the circulation fluid outlet and described circulation fluid spray equipment of described outer circular slot is provided with absorber portion outer circulation pump; The bottom discharging opening of described oxidation panel is connected with lower absorber portion outer circulation pump by lower absorber portion outer circulation pump feed pipe, lower absorber portion outer circulation pump is connected with absorbing liquid spray equipment in described tower by lower absorber portion outer circulation pump discharge nozzle, and lower absorber portion outer circulation pump pumps material branched pipe by lower absorber portion outer circulation and is connected with the absorbing liquid spray equipment in described air inlet flue with described oxidation trough respectively.
In order to the pH value of supervising device liquid everywhere, and accurately control the dosage of ammonia, need to be provided with acdity and basicity measuring meter throughout, acdity and basicity measuring meter can be arranged on equipment or pipeline, the pipeline that particularly can be connected in described outer circular slot or with outer circular slot is provided with the pH measurement instrument one measuring groove Inner eycle liquid pH value, the pipeline be connected in described oxidation trough or with oxidation trough is provided with the pH measurement instrument two measuring groove internal oxidition liquid pH value, described lower absorber portion outer circulation pump discharge place or the pipeline that is connected with lower absorber portion outer circulation pump discharge are provided with the pH measurement instrument three measuring oxidation panel discharging pH value.
The beneficial effects of the utility model:
1) the utility model is the innovating and developing on conventional ammonia ammonium sulphate process desulfur technology basis, in conjunction with the absorbability of ammonia to sulfur dioxide and the advantage of process optimization, the processes such as flue gas cooling, absorption, oxidation are completed with an absorption tower, and makes the electrochemical conditions that each process keeps best.Simplify technological process, reduce cost of investment and energy consumption, reduce the problems such as plant area area;
2) employing absorption tower is the absorption tower of tower cornice annular sieve plate, solve flue gas along tower wall escape situation, when not increasing sprinkle density near tower wall, increase liquid-gas ratio near tower wall, and absorption space near tower wall is utilized effectively, solve the difficult point that traditional desulfur technology flue gas is escaped along tower wall.
3) absorption tower oxidation panel and oxidation trough all adopt Inner guide bucket to force self-loopa, oxidation effect, reduce air capacity; Structure is simple, does not need machine power, and operation is reliable, decreases electric energy loss.
Accompanying drawing explanation
Fig. 1 is a kind of ammonia ammonium sulphate process flue gas desulfur device of the present utility model and schematic flow sheet;
Fig. 2 is a kind of annular sieve plate structural representation of the present utility model.
In figure, 1-fume desulfurating absorption tower (hereinafter referred to as absorption tower), 2-outer circular slot, 3-upper absorber portion outer circulation pump, absorber portion outer circulation pump under 4-, 5-oxidation trough, 6-annular sieve plate, 7-demister, 8-absorbing fluid collector, 10-air inlet flue, 11-absorbs tower reactor diversing bucket, 12-oxidation trough Inner guide bucket, 13-absorbs air sparger in tower reactor diversing bucket, air sparger in 14-oxidation trough Inner guide bucket, 15-absorption tower escape pipe, 16-water inlet pipe, 17-removes on absorption tower outer circulation barrel, 18-outer circular slot removes outer circulation pump line, 19-outer circular slot goes to absorption tower to manage, 20-enters to absorb tower reactor oxidation air pipe, 21-absorbs tower reactor and mends ammonia pipe, absorber portion outer circulation pump feed pipe under 22-, absorber portion outer circulation pump discharge nozzle under 23-, under 24-, material branched pipe is pumped in absorber portion outer circulation, 25-enters oxidation trough oxidation air pipe, 26-oxidation trough discharge nozzle, 27-deoxidation groove discharge nozzle, 28-removes absorption tower flue absorbing liquid pipe, 29-flue gas, 30-oxidation trough liquid level, 31-absorption tower liquid level, 32-enters oxidation trough ammonia pipe, 33-enters outer circular slot ammonia pipe, 34-absorbs tower reactor and mends ammonia pipe distributor, 35-outer circular slot cooling water pipe, 36-ring baffle, 37-annular sieve plate internal ring wall, 38-annular sieve plate external annulus, 39-sieve aperture, absorbing liquid spray equipment in 41-tower, 42-circulation fluid spray equipment, 43-water spray system, 44-absorbing liquid spray equipment, 45-pH measurement instrument one, 46-annular sieve plate two, 47-ring baffle two, 55-pH measurement instrument two, 56-annular sieve plate three, 57-ring baffle three, 65-pH measurement instrument three, 66-oxidation trough mends ammonia pipe distributor.
Detailed description of the invention
Below in conjunction with drawings and Examples, the utility model is described further, but following content does not form the restriction to the utility model protection domain.
As shown in Figure 1, this ammonia ammonium sulphate process flue gas desulfur device comprises fume desulfurating absorption tower 1 and outer circular slot 2, also can bag oxidation trough 5, comprises oxidation panel, pre-absorption section, outer circulation absorber portion, washing section and demist section in fume desulfurating absorption tower 1 from bottom to top.
Oxidation panel is positioned at bottom, absorption tower, discharging opening is provided with in the bottom of oxidation panel, this discharging opening is connected by the entrance of pipeline with lower absorber portion outer circulation pump 4, and the outlet of described lower absorber portion outer circulation pump 4 is connected with the entrance of absorbing liquid spray equipment 41 in the tower be located in described pre-absorption section by pipeline; Be provided with in oxidation panel and absorb tower reactor diversing bucket 11, absorbing tower reactor diversing bucket 11 when equipment runs is positioned under liquid level, this absorption tower reactor diversing bucket is formed primarily of the straight bucket of bottom and the loudspeaker bucket upwards expanded on top, bottom in absorption tower reactor diversing bucket 11 is provided with and absorbs air sparger 13 in tower reactor diversing bucket, absorbs air sparger 13 in tower reactor diversing bucket and is connected with the tower reactor oxidation air pipe 20 that enters to absorb in order to pass into air; Absorbing the outside of tower reactor diversing bucket 11 or be around provided with and absorb tower reactor and mend ammonia pipe distributor 34, absorbing tower reactor benefit ammonia pipe distributor 34 and mend ammonia pipe 21 with the absorption tower reactor passing into ammonia and be connected.
Middle part in fume desulfurating absorption tower 1 or middle and upper part are provided with absorbing fluid collector 8, it is pre-absorption section between oxidation panel and absorbing fluid collector 8, pre-absorption section is connected by floss hole with air inlet flue 10, is provided with annular sieve plate 6 in the pre-absorption section on floss hole.
As shown in Figure 2, annular sieve plate 6 is provided with multiple sieve aperture, the external annulus of annular sieve plate 6 and the tower wall compact siro spinning technology of pre-absorption section, the ring baffle 36 that internal ring wall and a vertical direction of annular sieve plate 6 are set up is connected, the downflow weir of the top looping sieve plate 6 of this ring baffle 36, the bottom of this ring baffle 36 forms flue gas hydraulic barrier.
The bottom of absorbing fluid collector 8 is provided with liquid outlet, and the partially liq that this liquid outlet goes outer circulation barrel 17 to be connected absorbing fluid collector is collected with described outer circular slot 2 by absorption tower imports in outer circular slot 2; The bottom of outer circular slot 2 is provided with circulation fluid outlet, circulation fluid spray equipment 42 is provided with in fume desulfurating absorption tower 1 on described liquid header 8, described circulation fluid spray equipment 42 to be exported with the circulation fluid of outer circular slot 2 by pipeline and is connected, and forms described outer circulation absorber portion between described absorbing fluid collector 8 and circulation fluid spray equipment 42; The water spray system 43 be connected with water inlet pipe 16 is provided with in washing section on described outer circulation absorber portion; Demister is provided with, such as demister 7 in demist section.
This device can not comprise oxidation trough 5, but the oxidation trough 5 that can improve oxidation effectiveness can be added in a kind of preferred version, also the oxidation trough Inner guide bucket 12 that structure is similar with absorbing tower reactor diversing bucket 11 can be provided with further in oxidation trough 5, this oxidation trough Inner guide bucket 12 is made up of the straight bucket of bottom and the loudspeaker bucket upwards expanded on top, and the bottom in described oxidation trough Inner guide bucket 12 is provided with and enters air sparger 14 in oxidation trough Inner guide bucket that oxidation trough oxidation air pipe 25 is connected; The outside of described oxidation trough Inner guide bucket 12 or around be provided with described enter the oxidation trough that is connected of oxidation trough ammonia pipe 32 mend ammonia pipe distributor 66.Described oxidation trough 5 is provided with the deoxidation groove discharge nozzle 27 be connected with described oxidation panel bottom; Oxidation trough discharge nozzle 26 is provided with in the bottom of described oxidation trough 5.
This device can comprise flue gas cooling zone further, such as in air inlet flue 10, be provided with the absorbing liquid spray equipment 44 making absorbing liquid and flue gas 29 co-current contact, this absorbing liquid spray equipment 44 is by removing absorption tower flue absorbing liquid pipe 28 and being connected with the outlet of lower absorber portion outer circulation pump 4.Air inlet flue 10 in order to pass into flue gas in absorption tower, and air inlet flue 10 is with level or angle obliquely, and preferably angle obliquely passes in pre-absorption section.In the preferred version of Fig. 1, air inlet flue 10 passes in pre-absorption section with angle obliquely.Be provided with absorbing liquid spray equipment 41 in tower in pre-absorption section on annular sieve plate 6, in this tower, absorbing liquid spray equipment 41 is connected by the outlet of pipeline with lower absorber portion outer circulation pump 4.
Annular sieve plate structure in this device is except can be applicable to pre-absorption section, also can be applicable to outer circulation absorber portion or washing section, such as be provided with annular sieve plate 2 46 in cyclic absorption section outside, this annular sieve plate 2 46 is provided with multiple sieve aperture, the external annulus of annular sieve plate 2 46 and the tower wall compact siro spinning technology of outer circulation absorber portion, the ring baffle 2 47 that internal ring wall and a vertical direction of annular sieve plate 2 46 are set up is connected, the downflow weir of the top looping sieve plate 2 46 of this ring baffle 2 47, the bottom of this ring baffle 2 47 forms flue gas hydraulic barrier.Annular sieve plate 3 56 can also be provided with in described washing section, this annular sieve plate 3 56 is provided with multiple sieve aperture, the external annulus of annular sieve plate 3 56 and the tower wall compact siro spinning technology of washing section, the ring baffle 3 57 that internal ring wall and a vertical direction of annular sieve plate 3 56 are set up is connected, the downflow weir of the top looping sieve plate 3 56 of this ring baffle 3 57, the bottom of this ring baffle 3 57 forms flue gas hydraulic barrier.
What the top of the outer circular slot 2 of this device was provided with to pass into ammonia enters outer circular slot ammonia pipe 33.Absorption tower escape pipe 15 is provided with at the top of fume desulfurating absorption tower 1.
Each pipeline in this device can be arranged by mode of the prior art, in a kind of preferred version, the pipeline between the circulation fluid outlet and described circulation fluid spray equipment 42 of outer circular slot 2 is provided with absorber portion outer circulation pump 3; The bottom discharging opening of oxidation panel is connected with lower absorber portion outer circulation pump 4 by lower absorber portion outer circulation pump feed pipe 22, lower absorber portion outer circulation pump 4 is connected with absorbing liquid spray equipment 41 in described tower by lower absorber portion outer circulation pump discharge nozzle 23, and lower absorber portion outer circulation pump 4 pumps material branched pipe 24 by lower absorber portion outer circulation and is connected with the absorbing liquid spray equipment 44 in described air inlet flue 10 with described oxidation trough 5 respectively.
In order to the pH value of supervising device liquid everywhere, and accurately control the dosage of ammonia, the pH measurement instrument 1 measuring groove Inner eycle liquid pH value can be provided with on the pipeline be connected in described outer circular slot 2 or with outer circular slot 2, the pipeline be connected in described oxidation trough 5 or with oxidation trough 5 is provided with the pH measurement instrument 2 55 measuring groove internal oxidition liquid pH value, in described lower absorber portion outer circulation pump 4 exit or export on the pipeline that is connected with lower absorber portion outer circulation pump 4 and be provided with the pH measurement instrument 3 65 measuring oxidation panel discharging pH value.
In equipment running process, after dedusting containing SO
2flue gas 29 typical temperature higher, enter before absorption tower 1 and need to reduce temperature.This device, by inlet flue duct 10, washs by the absorbing fluid after peroxidating of absorption tower 1 tower reactor.Wash liquid nozzles available spray in inlet flue duct 10, in the direction of ejecting liquid and inlet flue duct 10 containing SO
2flue gas 29 co-current contact, the water evaporation endothermic in wash liquid, reduces the temperature of flue gas 29, and cleaning solution is concentrated simultaneously.Go the flow-control in absorption tower flue absorbing liquid pipe 28 to leave temperature when inlet flue duct 10 enters absorption tower 1 at flue gas 29 and be reduced to below dew point.
After entering absorption tower 1 from the flue gas carrying absorbing fluid secretly of inlet flue duct 10, gas-liquid separation, gas upwards enters pre-absorption section, and liquid falls into tower reactor, i.e. oxidation panel.
The diversing bucket of tower reactor liquid level 31 times design special constructions.Absorbing tower reactor diversing bucket 11 top is the bellmouth orifice expanded, and bottom is straight barrel-shaped shape.At the oxidation air distributor 13 that the straight bucket low inside of diversing bucket 11 installs, the air of absorption tower reactor oxidation air pipe 20 is made to enter in the distributor of straight bucket lower position of diversing bucket 11, to cause inside and outside diversing bucket gas holdup difference in liquid, in water conservancy diversion liquid in bucket, gas holdup is high, in the outer liquid of diversing bucket, gas holdup is low, cause the differential static pressure of fluid, thus produce liquid circulation motion, make absorbing fluid circulation between inner sleeve and sleeve are outer reach the object of diffusion and mass transfer.Because Inner eycle method for oxidation structure is simple, do not need machine power, operation is reliable, decreases electric energy loss.Meanwhile, oxidation panel is used for oxidation and generates ammonium sulfate, the pH value decline of solution, and the ammonia absorbing tower reactor benefit ammonia pipe 21 enters tower reactor by absorbing tower reactor benefit ammonia pipe distributor 34, and the liquid circulation produced due to diversing bucket moves, and ammonia is diffused rapidly in absorbing liquid.Namely control the pH value of absorption tower 1 tower reactor solution fast.Absorb ammonia residual that tower reactor mends ammonia pipe 21 by detecting lower absorber portion outer circulation pump 4 and export or controlling with the pH value of the solution exported in the pipeline that is connected.Ammonia ammonium sulphate process flue gas desulfurization wishes that product is ammonium sulfate, in absorption tower process, forms (NH
4)
2sO
3-NH
4hSO
3-H
2the absorbing liquid system of O, NH in this absorbing liquid system
4hSO
3to SO
2not there is absorbability, (NH in this solution
4)
2sO
3have good absorbability to SO2, it is the main absorber in ammonia process.Ammoniacal liquor is to SO
2assimilation effect poor, NH in this solution
4hSO
3to SO
2not there is absorbability, so NH in solution
4hSO
3when reaching finite concentration, need process of taking measures, ammonia ammonium sulphate process flue gas desulphurization system, controlling absorbing liquid pH value is to keep (NH in solution
4)
2sO
3concentration.At the oxidation panel on absorption tower, form (NH
4)
2sO
4-(NH
4)
2sO
3-NH
4hSO
3-H
2the absorbing liquid system of O, due to oxidation, partly (NH
4)
2sO
3be oxidized to (NH
4)
2sO
4,absorbability is caused to decline, so optimal situation is that transfer part oxidizing process is to oxidation trough.
The diversing bucket of special construction is designed, i.e. oxidation trough Inner guide bucket 12 under oxidation trough 5 liquid level.This diversing bucket top is the bellmouth orifice expanded, and bottom is straight barrel-shaped shape.Air sparger 14 in the oxidation trough Inner guide bucket that the straight bucket lower position of diversing bucket is arranged, the air into oxidation trough oxidation air pipe 25 is made to enter in the distributor of straight bucket lower position of diversing bucket, to cause inside and outside diversing bucket gas holdup difference in liquid, in water conservancy diversion liquid in bucket, gas holdup is high, in the outer liquid of diversing bucket, gas holdup is low, cause the differential static pressure of fluid, thus produce liquid circulation motion, make absorbing fluid circulation between inner sleeve and sleeve are outer reach the object of diffusion and mass transfer.Because Inner eycle method for oxidation structure is simple, do not need machine power, operation is reliable, decreases electric energy loss.Meanwhile, oxidation panel is used for oxidation, and sulfite oxidation generates ammonium sulfate, ammonium bisulfite oxidation generates ammonium sulfate, and the pH value of solution declines, and the ammonia entering oxidation trough ammonia pipe 32 enters oxidation trough 5, due to the liquid circulation motion that diversing bucket produces, ammonia is diffused rapidly in absorbing liquid.Namely control the pH value of absorption tower 1 tower reactor solution fast, make ammonium hydrogen sulfate change into stable ammonium sulfate.The supplementary ammonia amount entering oxidation trough ammonia pipe 32 is detected by the pH value be arranged on oxidation trough 5 and controls.
Absorption tower 1 oxidation panel liquid enters lower absorber portion outer circulation pump 4 through lower absorber portion outer circulation pump feed pipe 22, and absorbing fluid circulation is squeezed into the pre-absorption section on absorption tower by lower absorber portion outer circulation pump discharge nozzle 23.The utility model is defined as pre-absorption section by the still liquid liquid level 31 on absorption tower 1 between absorbing fluid collector 8.Annular sieve plate structure of the present utility model (comprising annular sieve plate, annular sieve plate two, annular sieve plate three) is for solving flue gas wall flow problem, the ring baffle installed at annular sieve plate end mainly has two functions, baffle plate upper end is the downflow weir of annular sieve plate, and baffle plate lower end is the flue gas hydraulic barrier of annular sieve plate.Process is as follows: when flue gas upwards flows along absorbing tower wall, arrive annular sieve plate place to be obstructed, direction baffling in tower, portion gas is through sieve aperture, contact with the absorbing fluid by sieve aperture, portion gas arrives annular sieve plate end, under deflection plate effect, the flow direction changes direction flowing in downward backward tower into, contacts with the absorbing fluid under spray.The absorbing liquid flowed along tower wall in annular sieve plate top and part ejecting liquid, collect on annular sieve plate, by the setting of annular sieve plate end height of weir plate, the liquid that partially absorbs collected on annular sieve plate is flowed downward by sieve aperture, flue gas near scrubbing tower wall, makes the liquid that partially absorbs collected on annular sieve plate be flowed out by annular sieve plate end downflow weir.Like this, on annular sieve plate, flue gas flow is reduced, and sprinkle density is constant, and liquid-gas ratio increases; The gas-liquid contact in liquid layer and sieve aperture is had in annular sieve plate; Under annular sieve plate, because partially liq have passed sieve aperture, also carry out gas-liquid contact with the flue gas risen near tower wall, absorbed space and be utilized effectively.
Lower absorber portion outer circulation is pumped material branched pipe 24 and is divided into deoxidation groove discharge nozzle 27 and removes absorption tower flue absorbing liquid pipe 28, by oxidation trough discharge nozzle 26 desulfuration crystalline ammonium after the oxidation of absorbing fluid deoxidation groove 5.
Be cyclic absorption section between the absorbing fluid collector 8 on absorption tower 1 and circulation fluid spray equipment 42.At the liquid header 8 that cyclic absorption section is arranged, liquid will be partially absorbed and derive absorption tower 1 from side line, go outer circulation barrel 17 to flow into outer circular slot 2 through absorption tower, control by pH measurement instrument 1 ammonia amount flowing into outer circular slot 2 through pipeline, thus the pH value of control outer circular slot 2 in the reasonable scope; Outer circular slot 2 goes outer circulation pump line 18 to remove upper absorber portion outer circulation pump 3 through outer circular slot, and absorbing liquid goes absorption tower pipe 19 to loop back absorption tower 1 by outer circular slot after upper absorber portion outer circulation pump pressurization.
Part between circulation fluid spray equipment 42 and water spray system 43 is washing section.At washing section, the water of water inlet pipe 16, by the flue gas of spray washing after ammonia absorbs, washs the ammonium sulfate, ammonia etc. carried secretly in flue gas.Flue gas after water washing, enters demist section, removes the droplet carried secretly in flue gas.Flue gas after demist is discharged through absorption tower escape pipe 15.
To process 220t/h boiler smoke, its exhaust gas volumn 270000Nm
3/ h (operating mode exhaust gas volumn 398600m
3/ h), entrance flue gas temperature 125 DEG C, inlet flue gas SO
2concentration 2000mg/Nm
3, with the ammonia absorption of 5% (wt) concentration, the ammonia vol of pre-wash section and oxidation trough adds up to 2832kg/h, pre-wash section internal diameter φ 6.4m, flue gas mean flow rate 3.2m/s, annular sieve plate width 300mm., sieve-plate aperture ratio 8%, about 5700m
3/ h flue gas passes through sieve aperture, pre-wash section hollow bulb flue gas mean flow rate 4.13m/s.
Pre-wash section absorbing liquid 41 DEG C, PH=5.0-6.3, spraying layer 3 layers, spray annular sieve plate Ban Shang district, upper strata, the void tower district in the spray annular sieve plate of intermediate layer, lower floor's spray annular sieve plate beneath-plate zone, upper strata spray flux 167m
3/ h, intermediate layer spray flux 167m
3/ h, lower floor spray flux 167m
3/ h, average liquid-gas ratio is respectively 1:2386,1:2352,1:2386.If do not added annular sieve plate, same spray total amount is divided into spraying layer 3 layers, and average liquid-gas ratio is 1:2386.And spray annular sieve plate Ban Shang district, upper strata is near Ta Bi position, and liquid-gas ratio is greater than mean value.So the actual liquid-gas ratio increasing spray-absorption after design annular sieve plate.
Outer circulation absorber portion, operating mode exhaust gas volumn 343900m
3/ h, with the ammonia absorption of 5% (wt) concentration, outer circulation absorber portion ammonia vol 2832kg/h, flue gas flow rate 2.3m/s, absorption tower internal diameter φ 7.2m, spray flux adds up to 250m
3/ h, the effect of design annular sieve plate is with pre-absorption section.PH value 5.0-6.0, temperature 40 DEG C.
The technique water yield 9445kg/h of tower upper supplementary.Flue gas discharges in air after flap demister and electrostatic precipitator.
By coefficient of oxygen utilization 18%, being oxidized air capacity needed for absorption tower and oxidation trough calculate is 2320m
3/ h, because there being part oxygen in flue gas, actual demand is less than 2320m
3/ h, if do not established diversing bucket, actual motion passes into oxidation air amount 1600m
3/ h, after oxidation panel and oxidation trough establish diversing bucket, actual motion passes into air capacity 1360m3/h.Oxidation trough pH value is 6.2, and faintly acid operates, temperature < 60 DEG C.
Go out adsorption tower smoke temperature 50 C, exiting flue gas SO
2concentration≤100mg/Nm
3, desulfuration efficiency>=95%, oxygenation efficiency>=98%.
Although here described by certain or some particular arrangement and illustrate the utility model, but its object do not lie in the described details of restriction, because various amendment and structure modify may be had within the scope of patent requirements, do not depart from utility model spirit.
The utility model does not relate to the part prior art that maybe can adopt all same as the prior art and is realized.
Claims (10)
1. an ammonia ammonium sulphate process flue gas desulfur device, it is characterized in that it fume desulfurating absorption tower comprising hollow (1) and outer circular slot (2), described fume desulfurating absorption tower comprises oxidation panel from bottom to top in (1), pre-absorption section, outer circulation absorber portion, washing section and demist section, discharging opening is provided with in the bottom of described oxidation panel, this discharging opening is connected by the entrance of pipeline with lower absorber portion outer circulation pump (4), the outlet of described lower absorber portion outer circulation pump (4) is connected with the entrance of absorbing liquid spray equipment (41) in the tower be located in described pre-absorption section by pipeline, be provided with in described oxidation panel and absorb tower reactor diversing bucket (11), this absorption tower reactor diversing bucket is formed primarily of the straight bucket of bottom and the loudspeaker bucket upwards expanded on top, be provided with and enter to absorb air sparger (13) in absorption tower reactor diversing bucket that tower reactor oxidation air pipe (20) is connected absorbing the bottom in tower reactor diversing bucket (11), be provided with in the outside of described absorption tower reactor diversing bucket (11) and absorb tower reactor and mend the absorption tower reactor that ammonia pipe (21) is connected and mend ammonia pipe distributor (34), absorbing fluid collector (8) is provided with in described fume desulfurating absorption tower (1), it is described pre-absorption section between described oxidation panel and absorbing fluid collector (8), pre-absorption section is connected by floss hole with air inlet flue (10), annular sieve plate (6) is provided with in pre-absorption section on described floss hole, this annular sieve plate (6) is provided with multiple sieve aperture, the external annulus of annular sieve plate (6) and the tower wall compact siro spinning technology of pre-absorption section, the ring baffle (36) that the internal ring wall of annular sieve plate (6) is set up with a vertical direction is connected, the bottom of described absorbing fluid collector (8) is provided with liquid outlet, and this liquid outlet imports in outer circular slot (2) by the partially liq that absorption tower goes outer circulation barrel (17) to be connected to make absorbing fluid collector collect with described outer circular slot (2), the bottom of outer circular slot (2) is provided with circulation fluid outlet, circulation fluid spray equipment (42) is provided with in fume desulfurating absorption tower (1) on described liquid header (8), described circulation fluid spray equipment (42) to be exported with the circulation fluid of described outer circular slot (2) by pipeline and is connected, and forms described outer circulation absorber portion between described absorbing fluid collector (8) and circulation fluid spray equipment (42), the water spray system (43) be connected with water inlet pipe (16) is provided with in washing section on described outer circulation absorber portion, demister (7) is provided with in described demist section.
2. ammonia ammonium sulphate process flue gas desulfur device according to claim 1, it is characterized in that the edge up and down of described ring baffle (36) all exceeds described annular sieve plate (6), the downflow weir on top looping sieve plate (6) of this ring baffle (36), the bottom of this ring baffle (36) forms flue gas hydraulic barrier.
3. ammonia ammonium sulphate process flue gas desulfur device according to claim 1, it is characterized in that this device also comprises oxidation trough (5), described oxidation trough (5) is connected by the outlet of pipeline with described lower absorber portion outer circulation pump (4); Described oxidation trough (5) is provided with into oxidation trough ammonia pipe (32); Oxidation trough discharge nozzle (26) is provided with in the bottom of described oxidation trough (5).
4. ammonia ammonium sulphate process flue gas desulfur device according to claim 3, it is characterized in that being provided with oxidation trough Inner guide bucket (12) in described oxidation trough (5), this oxidation trough Inner guide bucket (12) is made up of the straight bucket of bottom and the loudspeaker bucket upwards expanded on top, and the bottom in described oxidation trough Inner guide bucket (12) is provided with and enters air sparger (14) in oxidation trough Inner guide bucket that oxidation trough oxidation air pipe (25) is connected; Be provided with in the outside of described oxidation trough Inner guide bucket (12) with described enter the oxidation trough that is connected of oxidation trough ammonia pipe (32) mend ammonia pipe distributor (66).
5. ammonia ammonium sulphate process flue gas desulfur device according to claim 1, is characterized in that described air inlet flue (10) passes in pre-absorption section with level or angle obliquely; In described air inlet flue (10), be provided with the absorbing liquid spray equipment (44) making absorbing liquid and flue gas (29) co-current contact, this absorbing liquid spray equipment (44) is connected by the outlet of pipeline with described lower absorber portion outer circulation pump (4).
6. ammonia ammonium sulphate process flue gas desulfur device according to claim 1, it is characterized in that being provided with annular sieve plate two (46) in described outer circulation absorber portion, this annular sieve plate two (46) is provided with multiple sieve aperture, the external annulus of annular sieve plate two (46) and the tower wall compact siro spinning technology of outer circulation absorber portion, the ring baffle two (47) that internal ring wall and a vertical direction of annular sieve plate two (46) are set up is connected.
7. ammonia ammonium sulphate process flue gas desulfur device according to claim 1, it is characterized in that in described washing section, be provided with annular sieve plate three (56), this annular sieve plate three (56) is provided with multiple sieve aperture, the external annulus of annular sieve plate three (56) and the tower wall compact siro spinning technology of washing section, the ring baffle three (57) that internal ring wall and a vertical direction of annular sieve plate three (56) are set up is connected.
8. the ammonia ammonium sulphate process flue gas desulfur device according to claim 6 or 7, it is characterized in that the edge up and down of described ring baffle two (47) all exceeds described annular sieve plate two (46), the downflow weir of the top looping sieve plate two (46) of ring baffle two (47), the bottom of this ring baffle two (47) forms flue gas hydraulic barrier; The edge up and down of described ring baffle three (57) all exceeds described annular sieve plate three (56), the downflow weir of the top looping sieve plate three (56) of ring baffle three (57), the bottom of this ring baffle three (57) forms flue gas hydraulic barrier.
9. the ammonia ammonium sulphate process flue gas desulfur device according to claim 3 or 5, is characterized in that being provided with the absorption tower escape pipe (15) that the flue gas after making process discharges fume desulfurating absorption tower (1) at the top of described fume desulfurating absorption tower (1); Pipeline between the circulation fluid outlet and described circulation fluid spray equipment (42) of described outer circular slot (2) is provided with upper absorber portion outer circulation pump (3); The bottom discharging opening of described oxidation panel is connected with lower absorber portion outer circulation pump (4) by lower absorber portion outer circulation pump feed pipe (22), lower absorber portion outer circulation pump (4) is connected with absorbing liquid spray equipment (41) in described tower by lower absorber portion outer circulation pump discharge nozzle (23), and lower absorber portion outer circulation pump (4) is pumped material branched pipe (24) by lower absorber portion outer circulation and is connected with the absorbing liquid spray equipment (44) in described air inlet flue (10) with described oxidation trough (5) respectively.
10. ammonia ammonium sulphate process flue gas desulfur device according to claim 9, the pipeline that to it is characterized in that in described outer circular slot (2) or be connected with outer circular slot (2) is provided with the pH measurement instrument one (45) measuring groove Inner eycle liquid pH value, the pipeline be connected in described oxidation trough (5) or with oxidation trough (5) is provided with the pH measurement instrument two (55) measuring groove internal oxidition liquid pH value, in described lower absorber portion outer circulation pump (4) exit or export on the pipeline that is connected with lower absorber portion outer circulation pump (4) and be provided with the pH measurement instrument three (65) measuring oxidation panel discharging pH value.
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|---|---|---|---|
| CN201520572150.XU CN204891578U (en) | 2015-08-03 | 2015-08-03 | Ammonia - ammonium sulfate method flue gas desulphurization device |
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|---|---|---|---|
| CN201520572150.XU CN204891578U (en) | 2015-08-03 | 2015-08-03 | Ammonia - ammonium sulfate method flue gas desulphurization device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105013313A (en) * | 2015-08-03 | 2015-11-04 | 中石化南京工程有限公司 | Flue gas desulfurization device based on ammonia-ammonium sulfate method |
| CN106268235A (en) * | 2016-09-28 | 2017-01-04 | 中石化节能环保工程科技有限公司 | Oil field fuel oil injection boiler tail gas desulfurization denitration processing system |
| CN107198942A (en) * | 2017-07-12 | 2017-09-26 | 楚雄滇中有色金属有限责任公司 | Reproduce relieving haperacidity at initial stage tail gas by ammonia method desulphurization system and its method of controlling operation thereof |
-
2015
- 2015-08-03 CN CN201520572150.XU patent/CN204891578U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105013313A (en) * | 2015-08-03 | 2015-11-04 | 中石化南京工程有限公司 | Flue gas desulfurization device based on ammonia-ammonium sulfate method |
| CN105013313B (en) * | 2015-08-03 | 2017-03-08 | 中石化南京工程有限公司 | A kind of ammoniacal ammonium sulphate method flue gas desulfurization device |
| CN106268235A (en) * | 2016-09-28 | 2017-01-04 | 中石化节能环保工程科技有限公司 | Oil field fuel oil injection boiler tail gas desulfurization denitration processing system |
| CN107198942A (en) * | 2017-07-12 | 2017-09-26 | 楚雄滇中有色金属有限责任公司 | Reproduce relieving haperacidity at initial stage tail gas by ammonia method desulphurization system and its method of controlling operation thereof |
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