CN105457479A - Flue gas desulphurization zero-emission resource disposal system and method - Google Patents
Flue gas desulphurization zero-emission resource disposal system and method Download PDFInfo
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- CN105457479A CN105457479A CN201511028672.4A CN201511028672A CN105457479A CN 105457479 A CN105457479 A CN 105457479A CN 201511028672 A CN201511028672 A CN 201511028672A CN 105457479 A CN105457479 A CN 105457479A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/507—Sulfur oxides by treating the gases with other liquids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/14—Magnesium hydroxide
- C01F5/20—Magnesium hydroxide by precipitation from solutions of magnesium salts with ammonia
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/402—Alkaline earth metal or magnesium compounds of magnesium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
Abstract
The invention provides a flue gas desulphurization zero-emission resource disposal system and method. The flue gas desulphurization zero-emission resource disposal system comprises a desulphurization tower, an oxidation tank, a dehydration machine, a filtrate tank, a backflow system and a reaction tank. The desulphurization tower stores and circulates magnesium hydrate slurry and enables the magnesium hydrate slurry to react with sulfur-containing smoke so as to obtain desulphurization waste water. The oxidation tank obtains the desulphurization waste water and enables the desulphurization waste water to perform reaction under the catalytic action of a catalyst so as to obtain a waste water treating fluid. The waste water treating fluid is dehydrated by a dehydration machine, a filter cake and filtrate are obtained, and the filter cake is directly discharged out. When the preset concentration is not reached, the filtrate flows into a filtrate tank and is delivered back to the desulphurization tower through the backflow system for cyclic use. When the preset concentration is reached, the filtrate reacts with liquid ammonia in the reaction tank so as to obtain recoverable magnesium hydrate and ammonium sulfate. The system adopts the mode of magnesium hydrate and ammonium sulfate preparation to replace a conventional magnesium desulphurization and recovery process, is high in economic benefit and achieves greater resource recycling and reusing. In addition, calcination is not needed, the process is simpler and more convenient, the cost is lower, and environmental pollution and resource waste are avoided.
Description
Technical field
The present invention relates to flue gas desulfurization technique technical field, particularly a kind of flue gas desulfurization zero-emission resource processing system and method.
Background technology
The mineral combustions such as colliery are still one of mankind's main path obtaining the energy in social development now.And this kind of technique is while providing heat energy, also create a large amount of SO
2with atmosphere pollutions such as flue dust.Flue gas desulfurization is the desulfurization method of unique large-scale commercial application in the world, technology maturation and reliable, mainly contains wet method, semidry method, dry method.Wet desulfurizing process is then current the most widely used desulfur technology.Wherein magnesium processes desulfurization is compared with the limestone-gypsum method flue gas desulfurization technique of existing extensive use, have desulfuration efficiency high, overcome fouling and clogging and avoid the reluctant problem of byproduct.This method has received as a kind of economical and practical and technology with bright market prospects and has paid close attention to widely and develop.
In existing magnesium method flue gas desulphurization technique, generally can be divided into method of reproduction according to disposing the later stage of desulfurization product, abandoning method and oxid-reclamatiom method:
Particularly, in method of reproduction, slurries mainly magnesium sulfite and the Adlerika flowed out after reaction in absorption tower.When requiring to regenerate magnesia, first needing purified solution, then carrying out concentrating, dry, and with fluid bed, dried magnesium sulfite and magnesium sulfate to be calcined under the condition of strict temperature control, regenerate magnesia and SO
2, the magnesia that calcining generates returns absorption system, collects the SO that purity is higher
2gas is admitted to sulfuric acid apparatus Sulphuric acid.Because the decomposition temperature of magnesium sulfate is higher than magnesium sulfite, therefore result in the high energy consumption of technique, simultaneously in order to improve magnesian quality, strictly calcining heat need be controlled, also need the oxidation adding inhibitor suppression magnesium sulfite, above-mentioned steps all makes operating cost and management difficulty significantly increase.
Method of abandoning also is called magnesium hydroxide method, its sulfur removal technology is similar to method of reproduction, difference is in method of reproduction, in order to reduce the calcining and decomposing temperature of desulfurization product, the oxidation of desulfurization absorbing liquid need be prevented, then must carry out forced oxidation and at utmost change magnesium sulfate into impel magnesium sulfite abandoning in method.Abandon the flue gas system of method, serum producing system and SO
2absorption system is identical with method of reproduction, slurries process is then be oxidized through forced-air blast by reacted slurries, then Separation of Solid and Liquid, be separated water outlet standard discharge, waste residue outward transport is disposed, the magnesium salts that this law produces in sweetening process is arranged outward with waste water, therefore needs when running by constantly supplementing magnesia in serum producing system.Directly carry out outer row because the desulfurization wastewater containing a large amount of magnesium salts is general not treated, easily cause environmental pollution, also there is the problem of the wasting of resources simultaneously.
Oxid-reclamatiom method refers to that desulfurization product is oxidized to magnesium sulfate to be reclaimed again.Its sulfur removal technology and method of reproduction similar, only different in the processing mode of desulfurizer slurry.The magnesium sulfite that sulfur dioxide and magnesium hydroxide generate after reacting in desulfurizing tower enters absorption tower prime cement liquid pool, from air blast toward slurry pool forced air supply, is oxidized to magnesium sulfate, then carries out filtering to remove insoluble impurity.Adlerika after removing impurities produces to obtain epsom salt through concentration crystallization step.The epsom salt reclaimed packs bunker after drying, and separation water outlet is transported to desulfurizing tower after then reclaiming and recycles.The recovery product economic benefit of the method is poor, compared with the recovery process of high cost investment, easily causes phenomenon unable to make ends meet.
Also exist desulfurizing byproduct recovery process complicated in said method, operating cost is comparatively large, easily causes environmental pollution and reclaims the problems such as product deficiency in economic performance.
Summary of the invention
The object of the present invention is to provide a kind of flue gas desulfurization zero-emission resource processing system and method, to solve existing magnesium method flue gas desulphurization technique complex process existing in practice, operating cost is high, regenerant can not make full use of, it is poor and easily cause the problem of environmental pollution to reclaim product economic benefit.
For achieving the above object, the invention provides a kind of flue gas desulfurization zero-emission resource processing system, comprising:
Desulfurizing tower, described desulfurizing tower is used for hydrogen storage magnesia slurry, and the described magnesium hydroxide slurry that circulates makes itself and sulfur-containing smoke gas react obtains desulfurization wastewater and desulfurization fume, and described desulfurization fume directly discharges;
Oxidation trough, described oxidation trough, for obtaining described desulfurization wastewater, is obtained by reacting wastewater treatment liquid to make described desulfurization wastewater under the effect of catalyst;
Dewaterer, described oxidation trough is connected with this dewaterer, and described dewaterer is for removing the slag in described wastewater treatment liquid, and to obtain filter cake and filtrate, described filter cake is directly discharged;
Filtrate receiver, described filtrate receiver is connected with described dewaterer, and described filtrate enters this filtrate receiver, and described filtrate receiver monitors the concentration of described filtrate, inputs reactive tank when concentration reaches preset value, otherwise input return-flow system;
Return-flow system, the described filtrate that described return-flow system is used for concentration not reach preset value returns to the use of described desulfurizing tower Inner eycle;
Reactive tank, described reactive tank reacts to obtain callable magnesium hydroxide and ammonium sulfate for the described filtrate and liquefied ammonia concentration being reached preset value.
Preferably, the bottom of described desulfurizing tower is provided with circulating slot, and described circulating slot is for storing described magnesium hydroxide slurry, and the smoke inlet place of described desulfurizing tower is provided with pre-cooler, and described pre-cooler is used for lowering the temperature to flue gas.
Preferably, also comprise absorbing liquid storage tank, be connected with pH meter and dosing pump, for hydrogen storage magnesium oxide solution, and by described pH meter and dosing pump to supplemental hydrogen magnesium oxide solution in described desulfurizing tower and oxidation trough.
Preferably, slurries in described desulfurizing tower are circulated by fluidic system, one end of described fluidic system is connected with a circulating pump, the other end is connected with the spray system in described desulfurizing tower and/or spraying system, described circulating pump flows into described fluidic system for driving slurries, and described fluidic system is again sprayed by described spray system and/or spraying system and/or is sprayed in desulfurizing tower to mix with flue gas after being mixed with air by described slurries.
Preferably, the bottom of described desulfurizing tower is provided with the first aerator, and the bottom of described oxidation trough is provided with the second aerator.
Preferably, described first aerator and/or the second aerator are air blast or rotary-cut mixed flow aerator.
Preferably, described catalyst is stored in a catalyst carrier, and described catalyst carrier is connected with described oxidation trough, and described catalyst is the compound of cobalt salt or cobalt salt and other transition metal salts.
Preferably, also comprise the dashpot be located between described oxidation trough and described dewaterer, described dashpot is connected with a tripolite solution groove, described dashpot is for obtaining described wastewater treatment liquid and making it and carry out sludge conditioning from the tripolite solution in tripolite solution groove, and the wastewater treatment liquid after conditioning inputs to described dewaterer again.
Preferably, described reactive tank is with ammonia tank and be connected, described ammonia tank is used for carrying liquefied ammonia in described reactive tank, the delivery outlet of described reactive tank is connected with the second dewaterer, described second dewaterer carries out dehydration to described concentrate and the reacted solution of liquefied ammonia and obtains magnesium hydroxide mud cake and ammonium sulfate, described ammonium sulfate inputs to a vaporising device, and described vaporising device is used for carrying out distillation to described ammonium sulfate and obtains solid ammonium sulfate.
Preferably, described vaporising device is connected with described return-flow system, described vaporising device is used for distilling described ammonium sulfate at the temperature of 110 DEG C ~ 170 DEG C, the evaporation water obtained returns to described desulfurizing tower Inner eycle by described return-flow system and uses, or described evaporation water reclaims use as other process waters.
Present invention also offers a kind of flue gas desulfurization zero-emission method for processing resource, be applied in above-mentioned flue gas desulfurization zero-emission resource processing system, specifically comprise the following steps:
S1: the sulfur-containing smoke gas after desulfurizing tower Inner eycle magnesium hydroxide slurry makes itself and precooling treatment reacts and obtains desulfurization wastewater and desulfurization fume, and wherein, desulfurization fume directly discharges;
S2: described desulfurization wastewater input oxidation trough is obtained by reacting wastewater treatment liquid under the effect of catalyst;
S3: dewater to described wastewater treatment liquid and obtain filter cake and filtrate, described filter cake is directly discharged;
S4: the concentration of monitoring described filtrate, inputs reactive tank when concentration reaches preset value, otherwise input return-flow system uses to return to described desulfurizing tower Inner eycle;
S5: filtrate concentration being reached preset value in described reactive tank and the liquefied ammonia added react, and obtain callable magnesium hydroxide and ammonium sulfate.
Preferably, described step S1 also comprises: adopt fluidic system loop slurry, and circulation time carries out circulation spraying and/or spray after being mixed into air to slurries.
Preferably, described step S2 also comprises: the wastewater treatment liquid obtained and tripolite solution are carried out sludge conditioning, molecule is condensed for bulky grain, then the wastewater treatment liquid after conditioning is carried out the operation of step S3.
Preferably, described step S1 also comprises: adopt the first aerator to carry out Air Exposure to magnesium hydroxide slurry; Described step S2 also comprises: adopt the second aerator to carry out Air Exposure to the liquid in oxidation trough.
Preferably, described step S5 also comprises, after the filtrate that described concentration reaches preset value and the liquefied ammonia added react, reacted solution is carried out dehydration and obtains magnesium hydroxide mud cake and ammonium sulfate, described magnesium hydroxide mud cake is directly discharged, adopt a vaporising device to carry out distillation to described ammonium sulfate at the temperature of 110 DEG C ~ 170 DEG C and obtain evaporation water and solid ammonium sulfate, wherein, evaporation water is again returned to the use of described desulfurizing tower Inner eycle by described return-flow system or is reclaimed as other process waters and uses.
Flue gas desulfurization zero-emission resource processing system provided by the invention has following technique effect:
(1) flow process of special slurries treatment process (preparing magnesium hydroxide and ammonium sulfate) is adopted to replace the step of conventional magnesium processes desulfurization recovery process, the recovery product obtained is the high-purity sulfuric acid ammonia and magnesium hydroxide that economic benefit is higher, realizes the recycling of resource more golden eggs.And without the need to calcining, technological operation is more easy, and cost is lower.
(2) take measure: a, flue gas desulphurization system circulation atomizer passgae and/or spray pipeline on set up fluidic system; B, in desulfurizing tower circulating slot and oxidation trough, set up high efficient aeration equipment; C, oxidation trough add new catalyst; D, set up the return-flow system of desulfurization wastewater at filtrate receiver.Those measure consolidation system accessory substance magnesium sulfites to the conversion of magnesium sulfate, and recycle in process the significantly lifting realizing magnesium sulfate concentration at desulfurization wastewater.
(3) return-flow system is set at filtrate receiver place, makes the dust and impurity etc. collected in sweetening process be able to discharge in system constantly, process can't be utilized and enrichment with filtrate cycle, greatly reduce the probability of the block such as pipeline and nozzle.From filtrate receiver, the waste water meeting concentration requirement is discharged, the concentration stabilize of magnesium sulfate in efflux wastewater can be ensured, existing slagging-off facility can be made full use of again, ensure the purity of magnesium sulfate in efflux wastewater, also can not the liquid level normal fluctuation in desulfurizing tower circulating slot be had an impact simultaneously.
(4) in technological process except the first order dehydration produce lime-ash mud cake except, all products can be accomplished to recycle, achieve desulfurization wastewater zero-emission and accessory substance high efficient resourcing, in addition, due to recycling of filtrate, desulphurization system technique water consumption declines to a great extent, and avoids environmental pollution and the wasting of resources.
Accompanying drawing explanation
Fig. 1 is flue gas desulfurization zero-emission resource processing system structure chart provided by the invention;
Fig. 2 is flue gas desulfurization zero-emission method for processing resource flow chart provided by the invention.
Detailed description of the invention
For better the present invention being described, hereby with a preferred embodiment, and accompanying drawing is coordinated to elaborate to the present invention, specific as follows:
As shown in Figure 1, flue gas desulfurization zero-emission resource processing system provided by the invention, comprising:
Desulfurizing tower 6, desulfurizing tower 6 is for hydrogen storage magnesia slurry, and recycle hydrogen magnesia slurry makes itself and sulfur-containing smoke gas react obtains desulfurization wastewater and desulfurization fume, and wherein, desulfurization fume directly discharges;
Oxidation trough 13, oxidation trough 13 is for obtaining above-mentioned desulfurization wastewater, and to make desulfurization wastewater be obtained by reacting wastewater treatment liquid under the catalytic action of catalyst, catalyst improves the transformation efficiency of magnesium sulfite;
First dewaterer 19, oxidation trough 13 is connected with this first dewaterer 19, and the first dewaterer 19 is for removing the slag in wastewater treatment liquid, and to obtain filter cake and filtrate, wherein, filter cake is directly discharged;
Filtrate receiver 21, filtrate receiver 21 is connected with the first dewaterer 19, and filtrate enters this filtrate receiver 21, and filtrate receiver 21 monitors the concentration of filtrate, inputs reactive tank 22 when concentration reaches preset value, otherwise input return-flow system 24;
Return-flow system 24, return-flow system 24 returns to desulfurizing tower 6 Inner eycle for filtrate concentration not being reached preset value and uses, and can realize the continuous lifting of the magnesium sulfate concentration in waste water in the process, significantly reduces the technique water consumption of flue gas desulphurization system simultaneously;
Reactive tank 22, reactive tank 22 reacts to obtain callable magnesium hydroxide and ammonium sulfate for the filtrate and liquefied ammonia concentration being reached preset value.
Particularly, the bottom of desulfurizing tower 6 is provided with circulating slot, and circulating slot is used for hydrogen storage magnesia slurry.This desulfurizing tower 6 controls to carry out moisturizing, to ensure that the solution in the circulating slot of desulfurizing tower 6 is in more suitable concentration by water compensating valve 2; The smoke inlet place of desulfurizing tower 6 is provided with pre-cooler 4, sulfur-containing smoke gas after dust removal process enters desulfurizing tower 6 through air-introduced machine, the slurries of component loops mix with flue gas at pre-cooler 4 place place, be cooled to comparatively be suitable for SO while increasing the humidity of flue gas to flue gas
2there is the temperature of chemical reaction, and remove the dust in partial fume further.In the present embodiment, pre-cooler comprises a precooling portion force (forcing) pump 3, water colod-application is in advance delivered to by this precooling portion force (forcing) pump 3 effect that smoke inlet is in pre-cooler 4 and mixes with flue gas.In other preferred embodiments, pre-cooler 4 can adopt additive method to carry out the precooling of flue gas, and the present invention is not particularly limited to this.
Desulfurizing tower 6 is also connected with a pH meter, and pH meter is connected with medicine system, and pH meter and dosing pump are connected with absorbing liquid storage tank 12, stores the magnesium hydroxide solution needing to be supplemented in absorbing liquid storage tank 12.PH meter is for monitoring the acid-base value of the magnesium hydroxide slurry in desulfurizing tower 6, medicine system is used for automatically controlling to export the dose in absorbing liquid storage tank 12 by circulating slot dosing valve 8 according to the monitoring information from pH meter, thus to apply in magnesium hydroxide solution to desulfurizing tower 6 in magnesium hydroxide slurry.And the dose in absorbing liquid storage tank 12 also controls to be delivered in oxidation trough 13, with the sufficient reacting in controlled oxidization groove 13 by oxidation trough dosing valve.
Desulfurizing tower 6 is connected with fluidic system 9, and one end of this fluidic system 9 is connected with a circulating pump 7, and the other end is connected with the spray system in described desulfurizing tower and/or spraying system, and this circulating pump 7 is connected with the circulating slot bottom desulfurizing tower 6.Slurries in desulfurizing tower 6 are circulated by this fluidic system 9, circulating pump 7 enters fluidic system 9 for driving slurry stream, and fluidic system 9 is undertaken spraying and/or being sprayed in desulfurizing tower to mix with flue gas by above-mentioned spray system and/or spraying system after being mixed with air by slurries.The slurries being mixed into air make magnesium sulfite in circulation line, complete conversion to magnesium sulfate, its aeration efficiency be the 2-3 of micro-pore aeration efficiency doubly, be the 4-6 of boring aeration efficiency doubly.Owing to being make use of the power resources of circulating pump 7 as jet and aeration, not only promoting nebulization, and saved extra aeration energy consumption.In addition, the bottom of the desulfurizing tower 6 in the present embodiment is provided with the first aerator 5, and the bottom of oxidation trough 13 is provided with the second aerator 14.Aerator in the present embodiment is rotary-cut mixed flow aerator, by using air blast to be rotary-cut mixed flow aerator air feed, make rotary-cut mixed flow aerator promote aeration efficiency on the one hand as a kind of high efficient aeration equipment, can avoid occurring that blocking causes the problems such as aeration inefficacy on the other hand.Wherein, rotary-cut mixed flow aerator is primarily of urceolus, central intake pipe, forward spiral board, reverse spiral board, current divider composition, central intake pipe is vertically built-in and its top has air inlet, forward spiral board and reverse spiral board and central intake pipe are fixed, and current divider is fixed on the bottom of central intake pipe.This rotary-cut mixed flow aerator has heavy caliber aeration opening, when aeration, the reactant liquor that can efficiently avoid in desulfurizing tower and oxidation trough blocks owing to there is slag, than existing conventional patch formula aerator and the close aerator better effects if of function.
Catalyst in the present embodiment is new catalyst: cobalt chloride, and cobalt chloride is stored in a catalyst carrier 15.Catalyst carrier 15 is connected with oxidation trough 13, and in other preferred embodiments, catalyst can also for being stored in the compound etc. of cobalt salt in catalyst carrier 15 or cobalt salt and other transition metal salts.
Dashpot 16 is also provided with between oxidation trough 13 and the first dewaterer 19, dashpot 16 is connected with a tripolite solution groove 17, dashpot 16 obtains from the reacted wastewater treatment liquid of oxidation trough and makes it and carry out sludge conditioning from the tripolite solution in tripolite solution groove 17, and the wastewater treatment liquid after conditioning is by inputing to the first dewaterer 19 again to dredge pump 18.By adding tripolite solution, making the molecule (flue dust and the interior contained impurity of absorbing liquid) existed in waste water be condensed into large particle, being conducive to follow-up dewatering and filtering.
And reactive tank 22 is with ammonia tank 23 and be connected, ammonia tank 23 for carrying liquefied ammonia in reactive tank 22, and the delivery outlet of reactive tank 22 is connected with the second dewaterer 26.The filtrate (also claiming concentrate in the present embodiment) that concentration reaches preset value inputs to the second dewaterer 26 with the reacted solution of liquefied ammonia through membrane pump 25, second dewaterer 26 pairs concentrate and the reacted solution of liquefied ammonia carry out dehydration and obtain magnesium hydroxide mud cake and ammonium sulfate, magnesium hydroxide mud cake is directly collected by bucket 27 and is discharged, can be used for configuration or the sale of front end desulfurizing agent, and ammonium sulfate inputs to a vaporising device 28.Vaporising device 28 crystallization under the evaporating temperature of 110 ~ 170 DEG C, gained solid product is ammonia sulfate crystal, can be used as resource reusing or sale, also distillation obtains evaporation water, wherein, vaporising device 28 also can be connected with return-flow system 24, and evaporation water also returns to desulfurizing tower 6 Inner eycle by return-flow system 24 and uses, or evaporation water is as other process waters.Return-flow system 24 in the present embodiment is a circulating pump, and this circulating pump is used for providing power to make liquid-circulating in desulfurizing tower 6.
As shown in Figure 2, the method uses above-mentioned flue gas desulfurization zero-emission resource processing system to carry out to flue gas desulfurization zero-emission method for processing resource provided by the invention, comprises step S1 ~ S5, specific as follows:
S1: the sulfur-containing smoke gas after desulfurizing tower Inner eycle magnesium hydroxide slurry makes itself and precooling treatment reacts and obtains desulfurization wastewater and desulfurization fume, and wherein, desulfurization fume directly discharges.
Particularly, adopt the slurries in fluidic system circulation desulfurization tower, and circulation time carries out circulation spraying and/or spray after being mixed into air to slurries.Slurries in circulating slot are delivered in the fluidic system 9 in the middle part of desulfurizing tower 6 via circulating pump 7, loop slurry with from below to up containing SO
2flue gas carry out reverse contact and fully reaction, SO wherein
2with the magnesium hydroxide reaction neutralization in circulation fluid, the magnesium sulfite that the catalyst (adding from oxidation trough) in solution makes major part generate is converted into magnesium sulfate, and other impurity also major part are removed by washing, and former flue-gas temperature will reduce further simultaneously.Neat stress after desulfurization is after demister 1 removes fine droplet, and through tower top smoke stack emission in air, the desulfurization wastewater after desulfurization is back in circulating slot.Wherein, the first aerator is also adopted to carry out Air Exposure to magnesium hydroxide slurry in the present embodiment.
S2: desulfurization wastewater is inputted oxidation trough and be obtained by reacting wastewater treatment liquid under the effect of catalyst.
The desulfurization wastewater of discharging in desulfurizing tower 6 circulating slot is delivered in oxidation trough 13, and its main component is magnesium sulfite and magnesium sulfate.Under the effect of low dosage new catalyst (being cobalt chloride in the present embodiment), can Efficient Conversion slightly soluble magnesium sulfite be magnesium sulfate by the second aerator 14.Slurries after oxidation flow in dashpot 16 again, and add tripolite solution and carry out sludge conditioning.Again the wastewater treatment liquid after conditioning is carried out the operation of step S3.
S3: dewater to wastewater treatment liquid and obtain filter cake and filtrate, filter cake is directly discharged.
The filter cake produced after mud after sludge conditioning is dewatered by dewaterer 19 transports outward disposal after being collected by bucket 20, filtrate then flows in filtrate receiver 21, and to be back in desulfurizing tower 6 by return-flow system 24 as make-up water and (can be back to demister system, water charging system, chilldown system).Dewaterer 19 makes the dust and impurity etc. collected in sweetening process be able to discharge in system constantly, can't utilize process and enrichment, greatly reduce the probability of the block such as pipeline and nozzle with filtrate cycle.
S4: the concentration of monitoring filtrate, inputs reactive tank when concentration reaches preset value, otherwise input return-flow system uses to return to desulfurizing tower Inner eycle.
The concentrate meeting concentration requirement is discharged by filtrate receiver 21, the concentration stabilize of outer row's concentrate can be ensured, existing slagging-off facility can be made full use of again, ensure the purity of outer row's concentrate, also can not the liquid level normal fluctuation in desulfurizing tower circulating slot be had an impact simultaneously.In addition, due to recycling of filtrate, desulphurization system technique water consumption declines to a great extent.
S5: filtrate concentration being reached preset value in reactive tank and the liquefied ammonia added react, and obtain callable magnesium hydroxide and ammonium sulfate.
After the concentrate reaching concentration is reacted with the liquefied ammonia from ammonia tank 23, reacted solution is sent into the second dewaterer 26 to carry out dehydration and obtain magnesium hydroxide mud cake and ammonium sulfate, magnesium hydroxide mud cake is directly discharged by bucket 27, this mud cake is highly purified magnesium hydroxide, can be used for configuration or the sale of front end desulfurizing agent.And ammonium sulfate inputs to vaporising device 28, carry out distillation and obtain evaporation water and solid ammonium sulfate.Specifically at the temperature of 110 ~ 170 DEG C, carry out evaporative crystallization, be preferably crystallization under the evaporating temperature of 130 ~ 150 DEG C.Wherein, solid product is ammonia sulfate crystal, can be used as resource reusing or sale.Evaporation water is again returned in desulfurizing tower 6 by return-flow system 24 and recycles as moisturizing, also can be used as other process waters.
The method improves the transformation efficiency of desulfurization side product magnesium sulfite to magnesium sulfate by using the fluidic system of installation and high efficient aeration system and desulfurization wastewater to recycle in process, improves the concentration of magnesium sulfate in desulfurization wastewater.In addition novel catalyst effectively can improve the transformation efficiency of magnesium sulfite.Carry out flue gas desulfurization byproduct disposal by the technique preparing magnesium hydroxide and ammonium sulfate, achieve the more effective recycling of resource.
The above; be only the specific embodiment of the present invention, but protection scope of the present invention is not limited thereto, any those skilled in the art is in the technical scope that the present invention discloses; the distortion do the present invention or replacement, all should be encompassed within protection scope of the present invention.Therefore, protection scope of the present invention should be as the criterion with the protection domain of described claim.
Claims (15)
1. a flue gas desulfurization zero-emission resource processing system, is characterized in that, comprising:
Desulfurizing tower, described desulfurizing tower is used for hydrogen storage magnesia slurry, and the described magnesium hydroxide slurry that circulates makes itself and sulfur-containing smoke gas react obtains desulfurization wastewater and desulfurization fume, and described desulfurization fume directly discharges;
Oxidation trough, described oxidation trough, for obtaining described desulfurization wastewater, is obtained by reacting wastewater treatment liquid to make described desulfurization wastewater under the effect of catalyst;
Dewaterer, described oxidation trough is connected with this dewaterer, and described dewaterer is for removing the slag in described wastewater treatment liquid, and to obtain filter cake and filtrate, described filter cake is directly discharged;
Filtrate receiver, described filtrate receiver is connected with described dewaterer, and described filtrate enters this filtrate receiver, and described filtrate receiver monitors the concentration of described filtrate, inputs reactive tank when concentration reaches preset value, otherwise input return-flow system;
Return-flow system, the described filtrate that described return-flow system is used for concentration not reach preset value returns to the use of described desulfurizing tower Inner eycle;
Reactive tank, described reactive tank reacts to obtain callable magnesium hydroxide and ammonium sulfate for the described filtrate and liquefied ammonia concentration being reached preset value.
2. flue gas desulfurization zero-emission resource processing system according to claim 1, it is characterized in that, the bottom of described desulfurizing tower is provided with circulating slot, described circulating slot is for storing described magnesium hydroxide slurry, the smoke inlet place of described desulfurizing tower is provided with pre-cooler, and described pre-cooler is used for lowering the temperature to flue gas.
3. flue gas desulfurization zero-emission resource processing system according to claim 1, it is characterized in that, also comprise absorbing liquid storage tank, be connected with pH meter and dosing pump, for hydrogen storage magnesium oxide solution, and by described pH meter and dosing pump to supplemental hydrogen magnesium oxide solution in described desulfurizing tower and oxidation trough.
4. flue gas desulfurization zero-emission resource processing system according to claim 1, it is characterized in that, slurries in described desulfurizing tower are circulated by fluidic system, one end of described fluidic system is connected with a circulating pump, the other end is connected with the spray system in described desulfurizing tower and/or spraying system, described circulating pump flows into described fluidic system for driving slurries, and described fluidic system is again sprayed by described spray system and/or spraying system and/or is sprayed in desulfurizing tower to mix with flue gas after being mixed with air by described slurries.
5. flue gas desulfurization zero-emission resource processing system according to claim 1 and 2, is characterized in that, the bottom of described desulfurizing tower is provided with the first aerator, and the bottom of described oxidation trough is provided with the second aerator.
6. flue gas desulfurization zero-emission resource processing system according to claim 5, is characterized in that, described first aerator and/or the second aerator are rotary-cut mixed flow aerator.
7. flue gas desulfurization zero-emission resource processing system according to claim 1 and 2, it is characterized in that, described catalyst is stored in a catalyst carrier, and described catalyst carrier is connected with described oxidation trough, and described catalyst is the compound of cobalt salt or cobalt salt and other transition metal salts.
8. flue gas desulfurization zero-emission resource processing system according to claim 1, it is characterized in that, also comprise the dashpot be located between described oxidation trough and described dewaterer, described dashpot is connected with a tripolite solution groove, described dashpot is for obtaining described wastewater treatment liquid and making it and carry out sludge conditioning from the tripolite solution in tripolite solution groove, and the wastewater treatment liquid after conditioning inputs to described dewaterer again.
9. flue gas desulfurization zero-emission resource processing system according to claim 1, it is characterized in that, described reactive tank is connected with ammonia tank, described ammonia tank is used for carrying liquefied ammonia in described reactive tank, the delivery outlet of described reactive tank is connected with the second dewaterer, described second dewaterer carries out dehydration to described concentrate and the reacted solution of liquefied ammonia and obtains magnesium hydroxide mud cake and ammonium sulfate, described ammonium sulfate inputs to a vaporising device, and described vaporising device is used for carrying out distillation to described ammonium sulfate and obtains solid ammonium sulfate.
10. flue gas desulfurization zero-emission resource processing system according to claim 8, it is characterized in that, described vaporising device is connected with described return-flow system, described vaporising device is used for distilling described ammonium sulfate at the temperature of 110 DEG C ~ 170 DEG C, the evaporation water obtained returns to described desulfurizing tower Inner eycle by described return-flow system and uses, or described evaporation water reclaims use as other process waters.
11. 1 kinds of flue gas desulfurization zero-emission method for processing resource, is characterized in that, are applied in the flue gas desulfurization zero-emission resource processing system described in claim 1 to 8 any one, specifically comprise the following steps:
S1: the sulfur-containing smoke gas after desulfurizing tower Inner eycle magnesium hydroxide slurry makes itself and precooling treatment reacts and obtains desulfurization wastewater and desulfurization fume, and wherein, desulfurization fume directly discharges;
S2: described desulfurization wastewater input oxidation trough is obtained by reacting wastewater treatment liquid under the effect of catalyst;
S3: dewater to described wastewater treatment liquid and obtain filter cake and filtrate, described filter cake is directly discharged;
S4: the concentration of monitoring described filtrate, inputs reactive tank when concentration reaches preset value, otherwise input return-flow system uses to return to described desulfurizing tower Inner eycle;
S5: filtrate concentration being reached preset value in described reactive tank and the liquefied ammonia added react, and obtain callable magnesium hydroxide and ammonium sulfate.
12. flue gas desulfurization zero-emission method for processing resource according to claim 11, it is characterized in that, described step S1 also comprises: adopt fluidic system loop slurry, and circulation time carries out circulation spraying and/or spray after being mixed into air to slurries.
13. flue gas desulfurization zero-emission method for processing resource according to claim 11 or 12, it is characterized in that, described step S2 also comprises: the wastewater treatment liquid obtained and tripolite solution are carried out sludge conditioning, molecule is condensed for bulky grain, then the wastewater treatment liquid after conditioning is carried out the operation of step S3.
14. flue gas desulfurization zero-emission method for processing resource according to claim 11, it is characterized in that, described step S1 also comprises: adopt the first aerator to carry out Air Exposure to magnesium hydroxide slurry; Described step S2 also comprises: adopt the second aerator to carry out Air Exposure to the liquid in oxidation trough.
15. flue gas desulfurization zero-emission method for processing resource according to claim 11 or 12 or 14, it is characterized in that, described step S5 also comprises, after the filtrate that described concentration reaches preset value and the liquefied ammonia added react, reacted solution is carried out dehydration and obtains magnesium hydroxide mud cake and ammonium sulfate, described magnesium hydroxide mud cake is directly discharged, adopt a vaporising device to carry out distillation to described ammonium sulfate at the temperature of 110 DEG C ~ 170 DEG C and obtain evaporation water and solid ammonium sulfate, wherein, evaporation water again returns to described desulfurizing tower Inner eycle by described return-flow system and uses or reclaim use as other process waters.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106938175A (en) * | 2017-04-07 | 2017-07-11 | 青岛农业大学 | One kind utilizes magnesium processes desulfurization product production high concentration SO2The apparatus and method of gas |
| CN107055886A (en) * | 2017-06-07 | 2017-08-18 | 江苏海容热能环境工程有限公司 | A kind of depth graded point salt technique |
| CN108479364A (en) * | 2018-05-04 | 2018-09-04 | 中国神华能源股份有限公司 | Drum gun turret pH value measuring system and bubble tower desulphurization system |
| BE1027253B1 (en) * | 2019-08-15 | 2020-11-30 | North China Electric Power Univ Baoding | Device and process for the catalytic oxidation of magnesium sulfite, cobalt nitrate catalyst / zsm-5 molecular sieve and process for the preparation thereof |
| CN113122724A (en) * | 2021-03-31 | 2021-07-16 | 衢州华友钴新材料有限公司 | Treatment process for recycling waste residues generated in nickel-cobalt hydrometallurgy |
| CN113634587A (en) * | 2021-08-25 | 2021-11-12 | 昆明理工大学 | Resource utilization method for desulfurization and sulfur by using magnesite |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000093739A (en) * | 1998-09-22 | 2000-04-04 | Techno Toriito:Kk | Treatment of magnesium sulfate-containing wastewater |
| CN101531384A (en) * | 2009-03-05 | 2009-09-16 | 六合天融（北京）环保科技有限公司 | Technique for preparing electronic grade magnesium hydrate and ammonium sulphate by cycle serum featuring in flue gas desulfurization by method of magnesium oxidization |
| CN201783298U (en) * | 2010-07-27 | 2011-04-06 | 河南金谷环保工程设备有限公司 | Wet flue gas desulfurization (FGD) jet oxidization device |
| CN103990360A (en) * | 2014-03-06 | 2014-08-20 | 华东理工大学 | Continuous concentration purification method for desulfurization by-product magnesium sulfate solution |
| CN205517223U (en) * | 2015-12-31 | 2016-08-31 | 上海世渊环保科技有限公司 | Flue gas desulfurization zero release money source processing system |
-
2015
- 2015-12-31 CN CN201511028672.4A patent/CN105457479B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000093739A (en) * | 1998-09-22 | 2000-04-04 | Techno Toriito:Kk | Treatment of magnesium sulfate-containing wastewater |
| CN101531384A (en) * | 2009-03-05 | 2009-09-16 | 六合天融（北京）环保科技有限公司 | Technique for preparing electronic grade magnesium hydrate and ammonium sulphate by cycle serum featuring in flue gas desulfurization by method of magnesium oxidization |
| CN201783298U (en) * | 2010-07-27 | 2011-04-06 | 河南金谷环保工程设备有限公司 | Wet flue gas desulfurization (FGD) jet oxidization device |
| CN103990360A (en) * | 2014-03-06 | 2014-08-20 | 华东理工大学 | Continuous concentration purification method for desulfurization by-product magnesium sulfate solution |
| CN205517223U (en) * | 2015-12-31 | 2016-08-31 | 上海世渊环保科技有限公司 | Flue gas desulfurization zero release money source processing system |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106938175A (en) * | 2017-04-07 | 2017-07-11 | 青岛农业大学 | One kind utilizes magnesium processes desulfurization product production high concentration SO2The apparatus and method of gas |
| CN106938175B (en) * | 2017-04-07 | 2019-05-21 | 青岛农业大学 | It is a kind of to produce high concentration SO using magnesium processes desulfurization product2The application method of the device of gas |
| CN107055886A (en) * | 2017-06-07 | 2017-08-18 | 江苏海容热能环境工程有限公司 | A kind of depth graded point salt technique |
| CN107055886B (en) * | 2017-06-07 | 2019-10-15 | 江苏海容热能环境工程有限公司 | A kind of depth graded divides salt technique |
| CN108479364A (en) * | 2018-05-04 | 2018-09-04 | 中国神华能源股份有限公司 | Drum gun turret pH value measuring system and bubble tower desulphurization system |
| BE1027253B1 (en) * | 2019-08-15 | 2020-11-30 | North China Electric Power Univ Baoding | Device and process for the catalytic oxidation of magnesium sulfite, cobalt nitrate catalyst / zsm-5 molecular sieve and process for the preparation thereof |
| CN113122724A (en) * | 2021-03-31 | 2021-07-16 | 衢州华友钴新材料有限公司 | Treatment process for recycling waste residues generated in nickel-cobalt hydrometallurgy |
| CN113122724B (en) * | 2021-03-31 | 2023-01-13 | 衢州华友钴新材料有限公司 | Treatment process for recycling waste residues generated in nickel-cobalt hydrometallurgy |
| CN113634587A (en) * | 2021-08-25 | 2021-11-12 | 昆明理工大学 | Resource utilization method for desulfurization and sulfur by using magnesite |
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