CN114534465A - Novel calcium method desulfurization method and device for flue gas - Google Patents
Novel calcium method desulfurization method and device for flue gas Download PDFInfo
- Publication number
- CN114534465A CN114534465A CN202210443907.XA CN202210443907A CN114534465A CN 114534465 A CN114534465 A CN 114534465A CN 202210443907 A CN202210443907 A CN 202210443907A CN 114534465 A CN114534465 A CN 114534465A
- Authority
- CN
- China
- Prior art keywords
- desulfurization
- flue gas
- reaction
- slurry
- regeneration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- 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
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- 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
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Treating Waste Gases (AREA)
Abstract
Discloses a novel calcium desulphurization method and a novel calcium desulphurization device for flue gas, wherein the method comprises the following steps: feeding the desulfurization absorption liquid into an absorption tower, absorbing sulfur dioxide in the flue gas by using the desulfurization absorption liquid in the absorption tower to perform desulfurization purification on the flue gas, and finally generating a desulfurization completion liquid; carrying out regeneration reaction on the regeneration reaction slurry and the desulfurization completion liquid in a regeneration device outside the absorption tower to generate a gaseous desulfurization active agent; carrying out a mixing reaction on the gas desulfurization active agent and the flue gas to carry out desulfurization purification on the flue gas, and finally generating a desulfurization completion liquid in an absorption tower; and circularly carrying out the regeneration reaction of the regeneration reaction slurry and the desulfurization completion liquid so as to circularly utilize the gaseous desulfurization active agent to carry out desulfurization and purification on the flue gas. According to the novel calcium method desulfurization method and the novel calcium method desulfurization device for the flue gas, the flue gas desulfurization efficiency is improved, the desulfurization cost is reduced, the maintenance and the repair of desulfurization equipment are reduced, and the sulfur-containing index of the desulfurized flue gas is ensured to be at a low level.
Description
Technical Field
The present disclosure relates generally to the field of environmental protection, and more particularly to a novel calcium desulfurization method and apparatus for flue gas.
Background
This section is intended to introduce the reader to various aspects of art, which may be related to various aspects of the present principles that are described and/or claimed below. This discussion is believed to be helpful in providing the reader with background information to facilitate a better understanding of the various aspects of the present principles. Accordingly, these statements are to be read in this light, and not as admissions of prior art.
In order to reduce the pollution of the flue gas discharged by the coal-fired boiler to the atmospheric environment, flue gas desulfurization is an indispensable important link so as to reduce the discharge amount of sulfur dioxide and protect the atmospheric environment. Flue gas desulfurization techniques can be broadly classified into dry, semi-dry, and wet methods according to the form of the final reaction product of desulfurization. The wet desulfurization technique is to remove SO in the flue gas by using alkaline absorbent solution2(ii) a The dry desulfurization technique is to adopt a powdery adsorbent to adsorb SO in the flue gas2(ii) a The semi-dry flue gas desulfurization technology integrates some advantages and characteristics of wet desulfurization and dry desulfurization. The dry desulfurization technology has the disadvantages of slow absorption and adsorption rate of sulfur dioxide, low desulfurization efficiency, large equipment and high investment; the semi-dry desulfurization technique has disadvantages in that the corrosion, clogging and abrasion of equipment are serious, and the stability and reliability of operation cannot be satisfactory; the wet desulphurization technology is a gas-liquid reaction, and the desulphurization reaction speed is high; at present, the wet desulphurization technology is the most mature and most applied desulphurization process in the world (about 90% of coal-fired boilers adopt wet desulphurization), and the limestone/lime-gypsum method is the most mature and widely used wet desulphurization technology in the current process. The method has the advantages that the desulfurizer (generally limestone/lime) is low in cost, and the desulfurization product is gypsum, so that the desulfurizer can be used as an industrial raw material to enter the society for circular economy. However, the flue gas desulfurization using the conventional limestone/lime-gypsum method has the following disadvantages: firstly, the desulfurization process is greatly influenced by the pH value of the desulfurization slurry, when the pH value of the desulfurization slurry is low, the desulfurization efficiency is low, the index of sulfur dioxide in the discharged flue gas is unstable and exceeds the standard easily, and when the pH value of the desulfurization slurry is high, the desulfurization pipeline and a system are easy to block, and the maintenance cost of desulfurization equipment is high; secondly, the ratio of the desulfurization liquid to the gas is too large, namely the amount of the desulfurization slurry required for desulfurizing unit flue gas is large, one reason for the problem is that the sulfur-containing desulfurization product generated in the desulfurization process is not separated and fixed, and the sulfur-containing desulfurization product is repeatedly circulated in the absorption tower, so that the power consumption of desulfurization equipment is high; thirdly, the desulfurizing agent is not separated from the desulfurization product, and the desulfurizing process is carried outThe desulfurizer contains desulfurization products, and the separated desulfurization products also contain unreacted desulfurizer, so that the utilization rate of the desulfurizer is low, and the desulfurization efficiency is low; fourthly, the limestone/lime-gypsum method desulfurization equipment has complex system, large occupied area, high one-time investment, inconvenient maintenance and high maintenance cost.
Aiming at the defects, the existing flue gas desulfurization technology needs to be improved, the flue gas desulfurization efficiency is improved, the desulfurization cost is reduced, the maintenance and the repair of desulfurization equipment are reduced, and the sulfur-containing index of the desulfurized flue gas is ensured to be at a low value.
Disclosure of Invention
The present inventors have noticed the above-mentioned disadvantages of the existing flue gas desulfurization technology, and developed a novel calcium desulfurization technology for flue gas, which has high desulfurization efficiency, and generates a byproduct, i.e., gypsum, having a purity much higher than that of gypsum generated by the conventional limestone/lime-gypsum method, compared to the conventional limestone/lime-gypsum method flue gas desulfurization technology.
According to an aspect of the present disclosure, a method for novel calcium desulphurization of flue gas is provided, which comprises: feeding the desulfurization absorption liquid into an absorption tower, absorbing sulfur dioxide in the flue gas by using the desulfurization absorption liquid in the absorption tower to perform desulfurization purification on the flue gas, and finally generating a desulfurization completion liquid; carrying out regeneration reaction on the regeneration reaction slurry and the desulfurization completion liquid in a regeneration device outside the absorption tower to generate a gaseous desulfurization active agent; carrying out mixed reaction on the gaseous desulfurization active agent and the flue gas to carry out desulfurization purification on the flue gas, and finally generating a desulfurization completion liquid in an absorption tower; and circularly carrying out the regeneration reaction of the regeneration reaction slurry and the desulfurization completion liquid so as to circularly utilize the gaseous desulfurization active agent to carry out desulfurization and purification on the flue gas.
According to another aspect of the present disclosure, a device for novel calcium desulphurization of flue gas is provided, comprising: the desulfurization pump is used for sending the desulfurization absorption liquid into the absorption tower, so that the desulfurization absorption liquid is used for absorbing sulfur dioxide in the flue gas in the absorption tower to carry out desulfurization purification on the flue gas, and finally, a desulfurization completion liquid is generated; the regeneration reaction device is arranged outside the absorption tower and generates a gaseous desulfurization active agent by utilizing the regeneration reaction slurry to carry out the regeneration reaction with the desulfurization completion liquid; the induced draft fan is used for introducing the generated gaseous desulfurization active agent into the absorption tower, so that the gaseous desulfurization active agent and the flue gas are subjected to mixed reaction, the flue gas is desulfurized and purified, and a desulfurization completion liquid is finally generated in the absorption tower; the regeneration reaction device circularly performs the regeneration reaction of the regeneration reaction slurry and the desulfurization completion liquid so as to circularly utilize the generated gaseous desulfurization active agent to perform desulfurization purification on the flue gas.
According to the novel calcium desulphurization method and device for the flue gas, a desulphurization mechanism of tower internal circulation, tower internal sulfur capture and tower external reaction reduction sulfur fixation is adopted, so that the desulfurized solution containing sulfite fully performs double decomposition chemical reaction with the modified sulfur fixation slurry outside the tower, the desulphurization active substances generated by the reaction are recycled, the generated calcium sulfite is aerated to generate calcium sulfate dihydrate (gypsum) precipitate, the gypsum is separated by a filter press device, and the clear water returns to a desulphurization pump for recycling.
Compared with the traditional limestone/lime-gypsum flue gas desulfurization technology, the novel calcium method and the novel calcium method for flue gas desulfurization have the following advantages: firstly, fully reacting the water solution containing sulfate radical products after desulfurization with the modified sulfur-fixing slurry outside the absorption tower, recycling the desulfurization active agent generated by the reaction for desulfurization, separating and precipitating calcium sulfite generated by the reaction, and feeding the separated clear water into the absorption tower for recycling; secondly, a mechanism of capturing sulfur in the tower and reacting and fixing sulfur outside the tower is adopted, so that the problems that a desulfurization pipeline and a desulfurization system are easy to block and an absorption tower is hung on the wall are solved, and the maintenance cost of the desulfurization system is reduced; thirdly, compared with the traditional limestone/lime-gypsum method, the method greatly reduces the lime consumption and the power consumption of the desulfurization equipment, namely greatly reduces the desulfurization cost; finally, the equipment system adopted by the novel calcium method flue gas desulfurization technology has the advantages of small occupied area, stable performance, low operating cost, convenient maintenance and strong adaptability to coal type change and load change.
Drawings
Other features, objects, and advantages of the disclosure will be from the following description, which is intended to be illustrative only and not limiting, and which must be read in connection with the accompanying drawings, wherein:
FIG. 1 is a schematic view showing an overall framework of a desulfurization system to which a conventional limestone-gypsum desulfurization technique is applied;
FIG. 2 is a block diagram of a desulfurization system utilizing the novel calcium desulfurization technique for flue gas in accordance with one embodiment of the present disclosure;
FIG. 3 is a flow diagram of a method for novel calcium desulfurization of flue gas according to an embodiment of the present disclosure;
fig. 4 is a block diagram of an apparatus for novel calcium desulfurization of flue gas according to an embodiment of the present disclosure.
Detailed Description
The subject matter is now described with reference to the drawings, wherein like reference numerals are used to refer to like elements throughout. In the following description, for purposes of explanation, numerous specific details are set forth in order to provide a thorough understanding of the subject matter. It may be evident, however, that the present principles may be practiced without these specific details.
This description illustrates the principles of the disclosure. It will thus be appreciated that those skilled in the art will be able to devise various arrangements that, although not explicitly described or shown herein, embody the principles of the disclosure.
The present principles are naturally not limited to the embodiments described herein.
It should be noted that references in the specification to "one embodiment," "an example embodiment," or "a particular embodiment" means that the embodiment described may include a particular feature, structure, or characteristic, but every embodiment may not necessarily include the particular feature, structure, or characteristic. Moreover, such phrases are not necessarily referring to the same embodiment. Further, when a particular feature, structure, or characteristic is described in connection with an embodiment, it is submitted that it is within the knowledge of one skilled in the art to effect such feature, structure, or characteristic in connection with other embodiments whether or not explicitly described.
As mentioned above, the conventional limestone/lime-gypsum flue gas desulfurization technique generally employs limestone (CaCO)3) Or lime (CaO) is used as a desulfurization absorbent, when limestone is used as an absorbent, the limestone is crushed and ground into powder and is mixed with water and stirred into absorbent slurry, and when lime is used as the absorbent, the lime powder is digested and then added with water to prepare the absorbent slurry; in the absorption tower, the absorption slurry is contacted and mixed with the flue gas, the sulfur dioxide in the flue gas is chemically reacted with the calcium carbonate in the slurry and the blown oxidizing air so as to be removed, and the final reaction product is gypsum.
Fig. 1 schematically shows the overall framework of a desulfurization system to which a conventional limestone-gypsum desulfurization technique is applied. The basic principle of the limestone-gypsum method desulfurization technology is that limestone is used as a desulfurizing agent, formed lime slurry is used as desulfurization absorption liquid to absorb sulfur dioxide in flue gas to generate calcium sulfite, and then the calcium sulfite is oxidized into calcium sulfate, and finally gypsum recovered as a byproduct can be generated. The desulfurization system mainly comprises a lime slurry preparation device, an absorption tower, a desulfurization product treatment device, a flue gas duct, a control device and the like. As shown in fig. 1, limestone from a limestone silo is ground and pulverized, for example, to form limestone powder, and water is added into a slurry tank and stirred to prepare a lime slurry; and pumping the prepared lime slurry into an absorption tower through a lime slurry pump. The removal of sulfur dioxide in the absorber is carried out as follows: pumping the prepared lime slurry into a circulating oxidation tank at the lower part of an absorption tower, injecting the lime slurry into the absorption tower from the upper part of the absorption tower, cooling sulfur-containing flue gas discharged from a coal-fired boiler, removing most of smoke dust (not shown in figure 1), entering the absorption tower from the bottom of the absorption tower, enabling the sulfur-containing flue gas to flow in the reverse direction with the lime slurry inside the absorption tower, carrying out liquid-gas contact reaction on the sulfur-containing flue gas by the lime slurry, enabling the lime slurry to become slurry containing calcium sulfite after absorbing sulfur dioxide, discharging the flue gas after absorption and purification into the atmosphere through a reheating device, and discharging the flue gas containing the calcium sulfite into the atmosphereThe slurry is forcibly oxidized in a circulating oxidation tank to generate calcium sulfate dihydrate (gypsum) slurry; the resulting gypsum slurry is discharged from the absorption tower and subjected to the steps of precipitation, filtration, separation, dehydration, etc., to finally obtain solid gypsum as a by-product. Therefore, in the whole limestone-gypsum method flue gas desulfurization process, the process of generating dihydrate gypsum through the physical and chemical reactions of dissolving, oxidizing and the like of sulfur dioxide and lime slurry as desulfurization absorption liquid is the core part of the process; the sulfur dioxide in the sulfur-containing flue gas is fully contacted with the circulating slurry liquid drops atomized by the spraying layer to be dissolved and absorbed and then oxidized, the slurry absorbing the sulfur dioxide is fully oxidized by air forcibly blown into a slurry tank at the bottom of the absorption tower to generate gypsum crystals, the slurry containing a large amount of grown gypsum crystals is discharged out of the absorption tower, and the processes are all completed in the absorption tower. The desulfurization process mainly comprises SO in the flue gas2Decomposed into H when meeting fog drops+And HSO3 ﹣Or SO3 2-And absorb Ca in the slurry2+Reaction to form Ca (HSO)3)2Or CaSO3，CaSO3Oxidation to CaSO4The two are very insoluble in water, and the SO is driven by the chemical driving force2Further dissolution, chain-locking reaction, passing through SO in flue gas2And the desulfurization is achieved by continuous reaction with the absorption slurry. However, in the operation process of the desulfurization process, because the removed desulfurization product is not fixedly separated, the desulfurization product is repeatedly circulated in the absorption tower, so that the liquid-gas ratio is large and is about 12-18L/m3The equipment investment is large, and the operation energy consumption cost is high; the pH value control condition is harsh, if the pH value of the desulfurization slurry in the tower is too high, lime solubility is low easily, gypsum crystals are difficult to grow, deposition and scaling in the tower are caused, desulfurization pipelines and systems are easy to block, gypsum filtration is difficult, the system is not operated normally, the system maintenance cost is high, if the pH value of the desulfurization slurry in the tower is too low, equipment corrosion is easy to cause, the desulfurization efficiency is low, and the sulfur dioxide index of the desulfurized flue gas is unstable; further, as described above, all the processes of sulfur capture, desulfurization, sulfur fixation and the like are performedThe process is completely finished in the absorption tower, the desulfurizing agent and the desulfurization product are not separated, the desulfurizing agent contains the desulfurization product in the desulfurization process, the separated desulfurization product contains the unreacted desulfurizing agent, the utilization rate of the desulfurizing agent is low, the desulfurization efficiency is low, the increase of particles is easily caused, and the limestone-gypsum method desulfurization equipment has the advantages of complex system, large floor area and high one-time investment.
The inventor of the application pays attention to the above problems in the existing limestone/lime-gypsum flue gas desulfurization technology, and provides a novel flue gas calcium desulfurization technology, which adopts a mode of tower internal circulation, tower internal sulfur capture and tower external reaction reduction sulfur fixation to enable the desulfurized solution containing sulfite to fully perform double decomposition chemical reaction with the modified sulfur fixation slurry outside the tower, the generated desulfurization active substances are recycled, the generated calcium sulfite generates calcium sulfate sediment through aeration, gypsum is separated by a filter press device, and the separated clear water returns to an absorption tower for recycling.
Specifically, according to the novel calcium desulphurization technology for the flue gas, provided by the disclosure, in order to avoid the blockage of equipment pipelines, the prepared lime slurry is only used for fixing sulfur outside the absorption tower and does not enter the absorption tower for capturing sulfur; the desulfurized absorbing liquid/clear water liquid which enters the absorption tower for sulfur capture does not contain a desulfurization product, the desulfurization absorbing liquid and/or the gaseous desulfurization active agent which is generated circularly are used for sulfur capture in the absorption tower, the desulfurized finishing liquid containing sulfate radicals and/or sulfite radicals and the modified solid sulfur slurry are subjected to regeneration reaction outside the tower, the two are subjected to double decomposition chemical reaction, the generated gaseous desulfurization active agent enters the absorption tower for continuous sulfur capture, the similar compatibility principle is utilized, the gas-gas combination is adopted, the desulfurization efficiency of the sulfur-containing flue gas is improved, and the sulfur dioxide which is not combined in the sulfur-containing flue gas is dissolved in the desulfurized absorbing liquid under certain pressure. In addition, according to an embodiment of the present disclosure, the slurry after the regeneration of the precipitated gaseous desulfurization active agent is aerated, precipitated, and filtered to separate gypsum as a solid-phase product and clean water as a liquid-phase product, and the separated clean water is sent to a desulfurization pump for recycling.
Fig. 2 is a block diagram of a desulfurization system applying the novel calcium desulfurization technique for flue gas according to an embodiment of the present disclosure. The working principle of the desulfurization system applying the novel calcium desulfurization technology for flue gas according to the embodiment of the present disclosure is described in detail with reference to fig. 2. As shown in fig. 2, the sulfur-containing flue gas enters the absorption tower through the induced draft fan after being dedusted, the sulfur-containing flue gas is desulfurized in the absorption tower, and the desulfurized flue gas is treated by wet static electricity and the like and then is discharged to the atmosphere from the absorption tower through the chimney. According to the embodiment of the disclosure, a desulfurizing agent is uniformly stirred by a stirring tank to form a desulfurizing absorption liquid, the desulfurizing absorption liquid is input into a storage tank and enters a desulfurizing pump according to a set proportion from the storage tank, and meanwhile, water in a sedimentation tank of the desulfurizing pump is mixed and enters an absorption tower for sulfur capture; in an absorption tower, reacting desulfurization absorption liquid with sulfur-containing flue gas entering the absorption tower, carrying out chemical reaction on sulfur dioxide in the flue gas and the desulfurization absorption liquid to form desulfurization completion liquid containing sulfate radicals and sulfite radicals, discharging the desulfurization completion liquid out of the absorption tower, entering a reaction tank in a regeneration reaction device, carrying out regeneration reaction on the desulfurization completion liquid and regeneration reaction slurry in the reaction tank, and generating regeneration completion slurry containing desulfurization active agents, calcium sulfate and calcium sulfite through the regeneration reaction serving as double decomposition reaction; and precipitating the desulfurization active agent from the regeneration completion slurry in a precipitation tank. Alternatively, boiler induced draft fan hot air/flue gas waste heat may be introduced into the reaction tank and/or the precipitation tank to promote greater precipitation of the desulfurization active agent. Optionally, gaseous desulfurization active agent is separated out from the separation tank, and is guided into the absorption tower, so that the gaseous desulfurization active agent and sulfur-containing flue gas are subjected to mixed reaction, a similar compatibility principle is utilized, gas-gas combination is adopted, so that the desulfurization and purification efficiency of the flue gas is improved, sulfur dioxide which is not combined in the flue gas is dissolved in desulfurization absorption liquid under certain pressure, and finally desulfurization completion liquid is generated in the absorption tower. As described above, the desulfurization completion liquid generated in the absorption tower is discharged out of the absorption tower, enters the regeneration reaction device outside the absorption tower, and the gaseous desulfurization active agent is separated out from the generated regeneration completion slurry containing the desulfurization active agent, calcium sulfate and calcium sulfite through the reaction tank and the separation tank of the regeneration reaction device, so that the desulfurization active agent can be recycled to perform desulfurization treatment on the flue gas, that is, the regeneration reaction of the regeneration reaction slurry and the desulfurization completion liquid is performed circularly, so that the flue gas is desulfurized and purified by recycling the gaseous desulfurization active agent, and the usage amount of the desulfurization absorption liquid pumped into the absorption tower is greatly reduced.
By way of example, the preparation device of the regeneration reaction slurry comprises a regeneration reactant stirring tank and a regeneration reaction slurry storage tank, and the slurry storage tank can be automatically controlled to enter the reaction tank in the regeneration reaction device according to a set proportion, so that the regeneration reaction slurry can fully react with the desulfurization completion liquid containing sulfate radicals and sulfite radicals discharged from the absorption tower.
By way of example, the desulfurizing agent in the present disclosure is ammonium bicarbonate, and the desulfurizing agent is uniformly dissolved in water by stirring to form a desulfurization absorption liquid, wherein the mass percentage concentration of the desulfurization absorption liquid is 15% -20%. Optionally, the desulfurizing agent is in the form of granules with a diameter of 1mm or less.
By way of example, the regeneration reaction slurry in this disclosure is a lime slurry. According to the embodiment of the disclosure, lime powder or crushed limestone can be added with water and stirred to prepare lime slurry, wherein the mass percentage concentration of the lime slurry is 15-30%.
Alternatively, both lump quicklime and powdered lime may be used to prepare a lime slurry, which may be made more uniform and prevented from settling by agitation.
Alternatively, the flow rate of the lime slurry fed to the reaction tank may be dynamically adjusted according to the amount of aqueous ammonium sulfate in the desulfurization completion liquid. As an example, controlling the flow rate of the lime slurry under conditions that satisfy the ammonium sulfate reaction can ensure the purity of the produced gypsum, reducing the lime usage.
As an example, the gaseous desulfurization active agent in the present disclosure is ammonia gas.
According to an embodiment of the disclosure, the desulfurization absorption liquid absorbs the sulfur-containing flue gas by spraying, and the reaction mainly comprises:
absorbing SO with ammonium bicarbonate solution2The main reaction comprises:
dissolving sulfur dioxide in water:
SO2+H2O → H2SO3
the flue gas generally contains a certain amount of oxygen, and side reactions can also occur in the solution:
H2SO3+1/2O2→H2SO4
H2SO3+2NH4HCO3→ (NH4)2SO3+2H2O+2CO2↑
H2SO4+2NH4HCO3 → (NH4)2SO4+2H2O+2CO2↑
(NH4)2SO3+SO2+H2O→2NH4HSO3
for sulfuric acid tail gas, a small amount of SO is contained3The following reactions occur:
2 (NH4)2SO3+SO3+H2O→ (NH4)2SO4+2NH4HSO3
the flue gas generally contains a certain amount of oxygen, and side reactions can also occur in the solution:
(NH4)2SO3+1/2O2→(NH4)2SO4
thus, the desulfurization completion liquid contains substances such as ammonium sulfate, ammonium sulfite, and ammonium bisulfite.
According to an embodiment of the disclosure, lime slurry is prepared from quicklime as regeneration reaction slurry, and the regeneration reaction slurry and desulfurization completion liquid are subjected to double decomposition reaction in a regeneration reaction device, wherein the reaction mainly comprises the following steps:
CaO+H2O→Ca(OH)2
(NH4)2SO3+Ca(OH)2 →CaSO3↓+2NH3↑+2H2O
(NH4)2SO4+Ca(OH)2 → CaSO4↓+2NH3↑+2H2O
2NH4HSO3+Ca(OH)2 →CaSO3↓+(NH4)2SO3 +2H2O
2NH4HSO3+O2 →2NH4HSO4
NH4HSO4+Ca(OH)2 →CaSO4↓+ NH3↑+2H2O
optionally, limestone is pulverized to prepare lime slurry as regeneration reaction slurry, and the lime slurry and the desulfurization completion liquid are subjected to double decomposition reaction in a regeneration reaction device, wherein the double decomposition reaction mainly comprises the following steps:
(NH4)2SO3+CaCO3 →CaSO3↓+2NH3↑+CO2↑+H2O
(NH4)2SO4+CaCO3 →CaSO4↓+2NH3↑+CO2↑+H2O
NH4HSO3+CaCO3 →CaSO3↓+NH3↑+CO2↑+H2O
as described above, the desulfurization completion liquid containing sulfate and/or sulfite after desulfurization is subjected to a regeneration reaction with the modified sulfur-fixing slurry, such as lime slurry, and the two undergo a metathesis chemical reaction, and the generated gaseous desulfurization active agent (such as ammonia) enters the absorption tower to capture sulfur continuously.
SO2+2NH3+H2O → (NH4)2SO3
The flue gas generally contains a certain amount of oxygen, and side reactions can also occur in the solution:
(NH4)2SO3+1/2O2→ (NH4)2SO4
after regeneration, aerating calcium sulfite generated in the slurry to generate calcium sulfate dihydrate (gypsum) precipitate, separating the gypsum by a filter press device, and returning clear water to the absorption tower for recycling, wherein the main reaction is as follows:
CaSO3+1/2O2→CaSO4
CaSO4+2H2O → CaSO4·2H2O
according to an embodiment of the present disclosure, the regeneration reaction device is set to have a temperature of 30 to 50 ℃ and a pressure of about 1500Pa so as to accelerate the metathesis reaction rate and the amount of the gaseous desulfurization active agent to be precipitated
Optionally, the lime slurry and the desulfurization completion liquid are stirred and heated in a reaction tank of the regeneration reaction device by using waste heat of the flue gas to promote the metathesis reaction.
Optionally, the regeneration completion slurry produced by the metathesis reaction is heated in a precipitation tank of a regeneration reaction apparatus using waste heat of the flue gas to precipitate a gaseous desulfurization active agent.
According to the embodiment of the disclosure, the generated desulfurization active agent is recycled, that is, the generated gaseous desulfurization active agent (ammonia gas) returns to the absorption tower to perform gas-gas mixing reaction with the sulfur-containing flue gas, calcium sulfite generated in the slurry after regeneration is aerated to generate calcium sulfate dihydrate (gypsum) precipitate, the gypsum is separated by the filter press equipment, and the clear water returns to the absorption tower to be recycled.
Optionally, the slurry after the regeneration of the separated gaseous desulfurization active agent is subjected to aeration, precipitation and filtration to separate gypsum serving as a solid-phase product and clean water serving as a liquid-phase product, and the separated clean water is sent to a desulfurization pump for recycling.
By way of example, the desulfurization mechanism of the tower internal circulation, the tower internal sulfur capture and the tower external reaction reduction sulfur fixation provided by the disclosure enables the solution containing sulfite after desulfurization and the modified sulfur fixation slurry to fully perform double decomposition chemical reaction, the desulfurization active material generated by the reaction is recycled, the generated calcium sulfite is aerated to generate calcium sulfate dihydrate (gypsum) precipitate, the gypsum is separated by a filter press device, and the clear water is returned to the absorption tower for recycling.
By way of example, taking the system for actually operating the novel calcium desulfurization scheme for flue gas of the present disclosure as an example, when a 40-ton coal-fired boiler is operated at full load, when coal with a sulfur content of 0.3% is combusted as fuel, the coal contains 3 kg sulfur per ton of coal, the flue gas contains about 2 kg sulfur, 4 kg sulfur dioxide is produced, the 40-ton coal-fired boiler consumes 5.6 tons coal per hour, 22.4 kg sulfur dioxide is produced, 560 kg of an aqueous solution containing 20% ammonium bicarbonate is required, or 747 kg of an aqueous solution containing 15% ammonium bicarbonate is required; for example, when coal with 1% of sulfur content is combusted, 10 kg of sulfur is contained in each ton of coal, the sulfur content in flue gas is about 6 kg, 12 kg of sulfur dioxide is produced, and 5.6 tons of coal is consumed in a 40-ton coal-fired boiler per hour, 56 kg of sulfur dioxide is produced, 1400 kg of 20% ammonium bicarbonate aqueous solution is needed, or 1867 kg of 15% ammonium bicarbonate aqueous solution is needed. Therefore, the concentration and/or flow rate of the desulfurization absorbing liquid fed into the absorption tower can be dynamically adjusted by monitoring the sulfur content of the flue gas based on the sulfur content of the coal. For example, when the sulfur content in the flue gas is increased, the concentration of the desulfurization absorption liquid can be correspondingly increased, and the flow rate of the desulfurization absorption liquid is kept unchanged; of course, when the concentration of the desulfurization absorption liquid is kept constant, the flow rate of the desulfurization absorption liquid can be increased accordingly. Similarly, when the sulfur content in the flue gas is reduced, the concentration of the desulfurization absorption liquid can be correspondingly reduced, and the flow of the desulfurization absorption liquid is kept unchanged; of course, when the concentration of the desulfurization absorbing solution is kept constant, the flow rate of the desulfurization absorbing solution can be reduced accordingly.
Correspondingly, the lime dosage can be determined as follows, taking the example that 1 ton of sulfur dioxide needs about 2.2 tons of lime for neutralization, the mass percent concentration of lime contained in the lime slurry is 15-30%, and the flow meter of the lime slurry is selected to be 100-2000 kg/h.
Alternatively, the flow rates of the desulfurization absorption liquid and lime slurry flow meters can be proportionally changed along with the sulfur content of the coal.
FIG. 3 is a flow chart of a method for novel calcium desulfurization of flue gas according to an embodiment of the present disclosure. As shown in fig. 3, the method comprises the steps of: s305, feeding the desulfurization absorption liquid into an absorption tower, absorbing sulfur dioxide in the flue gas by using the desulfurization absorption liquid in the absorption tower to perform desulfurization and purification on the flue gas, and finally generating a desulfurization completion liquid; s310, carrying out regeneration reaction on the regeneration reaction slurry and the desulfurization completion liquid in a regeneration device outside the absorption tower to generate a gaseous desulfurization active agent; s315, carrying out mixed reaction on the flue gas by using a gaseous desulfurization active agent to carry out desulfurization purification on the flue gas, and finally generating a desulfurization completion liquid in an absorption tower; and S320, circularly carrying out the regeneration reaction of the regeneration reaction slurry and the desulfurization completion liquid so as to circularly utilize the gaseous desulfurization active agent to carry out desulfurization and purification on the flue gas.
Optionally, the method for novel calcium desulphurization of flue gas proposed according to the present disclosure further comprises: adding water into the desulfurizer in a stirring tank and stirring to prepare desulfurization absorption liquid; and sending the desulfurization absorption liquid into the absorption tower by using a desulfurization pump to absorb sulfur dioxide in the flue gas.
Alternatively, according to the method set forth in this disclosure, the regeneration reaction slurry is a lime slurry; the method further comprises the following steps: adding water into lime powder or crushed limestone and stirring to prepare lime slurry, wherein the mass percentage concentration of the lime slurry is 15-30%; and carrying out double decomposition reaction on the prepared lime slurry and the desulfurization completion liquid in a regeneration reaction device to generate regeneration completion slurry, and separating the gaseous desulfurization active agent from the regeneration completion slurry.
Optionally, a method is proposed according to the present disclosure, wherein the regeneration reaction device comprises a reaction tank and a precipitation tank, the method further comprising: stirring and heating the lime slurry and the desulfurization completion liquid in a reaction tank by using waste heat of flue gas to promote the double decomposition reaction; and heating the regeneration completion slurry generated by the double decomposition reaction by using the waste heat of the flue gas in an extraction tank to separate out the gaseous desulfurization active agent.
Alternatively, the method provided by the present disclosure, wherein the slurry after the regeneration of the separated gaseous desulfurization active agent is subjected to aeration, sedimentation and filtration to separate gypsum as a solid phase product and clean water as a liquid phase product, and the separated clean water is sent to a desulfurization pump for recycling.
Optionally, the method provided by the present disclosure, wherein the desulfurizing agent includes ammonium bicarbonate, the mass percentage concentration of the desulfurization absorption liquid is 15% to 20%, and the gaseous desulfurization active agent is ammonia gas.
Optionally, the method proposed according to the present disclosure further includes: and dynamically adjusting the flow and/or concentration of the desulfurization absorption liquid fed into the absorption tower according to the sulfur content of the flue gas.
Fig. 4 is a block diagram of an apparatus for novel calcium desulfurization of flue gas according to an embodiment of the present disclosure. As shown in fig. 4, the apparatus includes: the desulfurization pump 401 is used for sending the desulfurization absorption liquid into the absorption tower, so that the desulfurization absorption liquid is used for absorbing sulfur dioxide in the flue gas in the absorption tower to carry out desulfurization purification on the flue gas, and finally a desulfurization completion liquid is generated; a regeneration reaction device 402 disposed outside the absorption tower, which generates a gaseous desulfurization active agent by performing a regeneration reaction between the regeneration reaction slurry and the desulfurization completion liquid; the induced draft fan 403 is used for introducing the generated gaseous desulfurization active agent into the absorption tower, so that the gaseous desulfurization active agent and the flue gas are subjected to mixing reaction, the flue gas is desulfurized and purified, and a desulfurization completion liquid is finally generated in the absorption tower; the regeneration reaction device circularly performs the regeneration reaction of the regeneration reaction slurry and the desulfurization completion liquid so as to circularly utilize the generated gaseous desulfurization active agent to perform desulfurization purification on the flue gas.
Optionally, an apparatus according to the present disclosure is provided, wherein the regeneration reaction is a metathesis reaction of the regeneration reaction slurry and the desulfurization completion liquid in a regeneration reaction apparatus to generate a regeneration completion slurry, wherein the regeneration reaction apparatus includes a reaction tank and a precipitation tank, the reaction tank uses waste heat of the flue gas to stir and heat the regeneration reaction slurry and the desulfurization completion liquid to promote the metathesis reaction, and the precipitation tank uses waste heat of the flue gas to heat the regeneration completion slurry generated by the metathesis reaction to precipitate the gaseous desulfurization active agent.
Optionally, according to the above apparatus proposed by the present disclosure, adding water to the desulfurizing agent in the stirring tank and stirring to prepare a desulfurization absorption liquid; and sending the desulfurization absorption liquid into the absorption tower by using a desulfurization pump to absorb sulfur dioxide in the flue gas.
Optionally, according to the above-mentioned apparatus proposed by the present disclosure, the regeneration reaction slurry is a lime slurry; adding water into lime powder or crushed limestone and stirring to prepare lime slurry, wherein the mass percentage concentration of the lime slurry is 15-30%; and carrying out double decomposition reaction on the prepared lime slurry and the desulfurization completion liquid in a regeneration reaction device to generate regeneration completion slurry, and separating the gaseous desulfurization active agent from the regeneration completion slurry.
Optionally, the above apparatus proposed by the present disclosure, wherein the slurry obtained by regenerating the precipitated gaseous desulfurization active agent is subjected to aeration, sedimentation, and filtration to separate gypsum as a solid phase product and clean water as a liquid phase product, and the separated clean water is sent to the desulfurization pump for recycling.
Optionally, according to the above apparatus provided by the present disclosure, the desulfurizing agent includes ammonium bicarbonate, the mass percentage concentration of the desulfurization absorption liquid is 15% to 20%, and the gaseous desulfurization active agent is ammonia gas.
Optionally, the above apparatus proposed according to the present disclosure further includes: and dynamically adjusting the flow and/or concentration of the desulfurization absorption liquid fed into the absorption tower according to the sulfur content of the flue gas.
By way of example, after the novel calcium desulphurization technology for flue gas provided by the embodiment of the disclosure is adopted in the desulphurization system of the coal-fired boiler experimental unit, the sulfur dioxide index of the flue gas after desulphurization is single digit for a long time and is basically maintained at 1mg/m3The environmental protection index is stable.
According to the technical scheme of the novel calcium method desulfurization of the flue gas, the method has the following characteristics:
1. the desulfurized completion liquid containing sulfate radicals and sulfite radicals is fully reacted with the modified sulfur-fixing slurry outside the absorption tower, the desulfurization active agent generated by the reaction is repeatedly desulfurized and used, the generated calcium sulfate and calcium sulfite are separated and precipitated, and the separated clear water enters the absorption tower to be repeatedly recycled;
2. the mode of sulfur capture in the tower and sulfur fixation reaction outside the tower provided by the disclosure thoroughly solves and avoids the phenomena of blockage of a desulfurization pipeline and a desulfurization system and wall hanging of the desulfurization tower;
3. compared with the traditional lime gypsum method desulfurization mode, the technical scheme provided by the disclosure greatly reduces the lime consumption and the power consumption of desulfurization equipment;
4. the novel calcium method flue gas desulfurization technical equipment system is simple and tidy, small in occupied area, stable in performance, low in operating cost, convenient to maintain and strong in adaptability to coal type changes and load changes.
Taking a 100-ton coal-fired boiler as an example, adopting a traditional lime-gypsum method desulfurization mode, arranging four layers of spraying in a desulfurization tower, wherein the lift of a desulfurization water pump is 25 meters, the water quantity of each layer is 600 square meters, the power of the water pump is 110 kilowatts, the total power of the four layers is generally more than 450KW, the daily power consumption is about 10800 degrees, and 3-5 tons of desulfurizer (lime) are adopted; by adopting the novel calcium desulphurization technology for the flue gas, the total power of a desulphurization water pump is less than 100KW, the daily power consumption is 1800 ℃, and about 1 ton of lime with 83% of calcium content of a desulfurizer is needed.
In addition, the index of sulfur dioxide contained in the flue gas after desulfurization by the novel calcium method desulfurization technology of the flue gas is single digit for a long time and is basically maintained at 1mg/m3And the PH value of the desulfurization absorption liquid is controlled to work at a low value all the time, so that the blockage of a desulfurization pipeline caused by the high PH value of the desulfurization liquid is avoided, the maintenance cost of desulfurization equipment is greatly reduced, the operation cost is reduced, the power consumption is reduced to more than 1/3 of the original power consumption, and the lime consumption is reduced to more than 1/3 of the original power consumption.
As will be appreciated by one skilled in the art, the embodiments described herein may be implemented, for example, by a method or process, an apparatus, a computer program product, a data stream, or a signal. Even if only a single embodiment is discussed in the context (e.g., as a method or device), embodiments of the features discussed may be implemented in other forms (e.g., a program). An apparatus may be implemented in, for example, appropriate hardware, software, and firmware. The method may be implemented in, for example, an apparatus such as a processor, which refers generally to a processing device including, for example, a computer, microprocessor, integrated circuit, or programmable logic device. Processors also include communication devices, such as smart phones, tablets, computers, cell phones, portable/personal digital assistants ("PDAs"), and other devices that facilitate the communication of information between end-users.
Additionally, the methods may be implemented by instructions being executed by a processor, and such instructions (and/or data values resulting from the implementation) may be stored in a processor-readable medium, such as an integrated circuit, software carrier, or other storage device; other storage devices may be, for example, a hard disk, a Compact Disc (CD), an optical disc (e.g., DVD, commonly referred to as a digital versatile disc or a digital video disc), a Random Access Memory (RAM), or a Read Only Memory (ROM). The instructions may form an application program tangibly embodied on a processor-readable medium. The instructions may be in, for example, hardware, firmware, software, or a combination thereof. The instructions may be found in, for example, an operating system, a separate application, or a combination of both. Thus, a processor may be characterized, for example, as a device configured to perform a process and a device including a processor-readable medium (such as a storage device) having instructions for performing a process. Further, a processor-readable medium may store data values produced by an embodiment in addition to or in place of instructions.
A number of embodiments have been described. Nevertheless, it will be understood that various modifications may be made. For example, elements of different embodiments may be combined, supplemented, modified, or removed to produce other embodiments. In addition, it will be appreciated by those of ordinary skill in the art that other structures and processes may be substituted for the disclosed structures and processes, and that the resulting embodiments will perform at least substantially the same function in at least substantially the same way to achieve at least substantially the same result as the disclosed embodiments. Thus, these and other embodiments are contemplated by this application.
The various embodiments described above can be combined to provide further embodiments. Aspects of the embodiments can be modified, if necessary to employ concepts of the various patents, applications and publications to provide yet further embodiments.
These and other changes can be made to the embodiments in light of the above detailed description. In general, in the following claims, the terms used should not be construed to limit the claims to the specific embodiments disclosed in the specification and the claims, but should be construed to include all possible embodiments along with the full scope of equivalents to which such claims are entitled. Accordingly, the claims are not limited by the disclosure.
Claims (9)
1. A novel calcium desulphurization method for flue gas comprises the following steps:
feeding the desulfurization absorption liquid into an absorption tower, absorbing sulfur dioxide in the flue gas by using the desulfurization absorption liquid in the absorption tower to perform desulfurization purification on the flue gas, and finally generating a desulfurization completion liquid, wherein the desulfurization absorption liquid is an ammonium bicarbonate solution;
carrying out regeneration reaction on the regeneration reaction slurry and the desulfurization completion liquid in a regeneration device outside the absorption tower to generate a gaseous desulfurization active agent, wherein the regeneration reaction slurry is lime slurry, and the gaseous desulfurization active agent is ammonia gas;
carrying out mixed reaction on the gaseous desulfurization active agent and the flue gas to carry out desulfurization purification on the flue gas, and finally generating a desulfurization completion liquid in an absorption tower; and
and circularly carrying out the regeneration reaction of the regeneration reaction slurry and the desulfurization completion liquid so as to circularly utilize the gaseous desulfurization active agent to carry out desulfurization and purification on the flue gas.
2. The method of claim 1, wherein,
adding water into the desulfurizer in a stirring tank and stirring to prepare desulfurization absorption liquid; and
and (3) feeding desulfurization absorption liquid into the absorption tower by using a desulfurization pump to absorb sulfur dioxide in the flue gas, wherein the desulfurizer is ammonium bicarbonate.
3. The method of claim 1, further comprising:
adding water into lime powder or crushed limestone and stirring to prepare lime slurry, wherein the mass percent concentration of the lime slurry is 15-30%; and
and carrying out double decomposition reaction on the prepared lime slurry and the desulfurization completion liquid in a regeneration reaction device to generate regeneration completion slurry, and separating the gaseous desulfurization active agent from the regeneration completion slurry.
4. The method of claim 3, wherein the regeneration reaction device comprises a reaction tank and a precipitation tank, the method further comprising:
stirring and heating the lime slurry and the desulfurization completion liquid in a reaction tank by using waste heat of flue gas to promote the double decomposition reaction; and
and heating the regeneration completion slurry generated by the double decomposition reaction by using the waste heat of the flue gas in a precipitation tank to precipitate the gaseous desulfurization active agent.
5. The method as claimed in claim 4, wherein the slurry after the regeneration of the separated gaseous desulfurization active agent is aerated, precipitated and filtered to separate gypsum as a solid phase product and clean water as a liquid phase product, and the separated clean water is sent to a desulfurization pump for recycling.
6. The method of any one of claims 1 to 5, wherein the desulfurization absorption liquid has a mass percentage concentration of 15% to 20%.
7. The method of any of claims 1-5, further comprising:
and dynamically adjusting the flow and/or concentration of the desulfurization absorption liquid fed into the absorption tower according to the sulfur content of the flue gas.
8. A device for novel calcium method of flue gas desulfurization includes:
the desulfurization pump is used for sending the desulfurization absorption liquid into the absorption tower, so that the desulfurization absorption liquid is used for absorbing sulfur dioxide in the flue gas in the absorption tower to carry out desulfurization purification on the flue gas, and finally, a desulfurization completion liquid is generated, wherein the desulfurization absorption liquid is an ammonium bicarbonate solution;
the regeneration reaction device is arranged outside the absorption tower and generates a gaseous desulfurization active agent by utilizing the regeneration reaction slurry and the desulfurization completion liquid to carry out regeneration reaction, wherein the regeneration reaction slurry is lime slurry, and the gaseous desulfurization active agent is ammonia gas; and
the induced draft fan is used for introducing the generated gaseous desulfurization active agent into the absorption tower, so that the gaseous desulfurization active agent and the flue gas are subjected to mixed reaction, the flue gas is desulfurized and purified, and finally desulfurization completion liquid is generated in the absorption tower;
the regeneration reaction device circularly performs the regeneration reaction of the regeneration reaction slurry and the desulfurization completion liquid so as to circularly utilize the generated gaseous desulfurization active agent to desulfurize and purify the flue gas.
9. The apparatus of claim 8, wherein the regeneration reaction is a metathesis reaction of the regeneration reaction slurry and the desulfurization completion liquid in a regeneration reaction apparatus to produce a regeneration completion slurry, wherein the regeneration reaction apparatus comprises a reaction tank and a precipitation tank, the reaction tank uses waste heat of flue gas to stir and heat the regeneration reaction slurry and the desulfurization completion liquid to promote the metathesis reaction, and the precipitation tank uses waste heat of flue gas to heat the regeneration completion slurry produced by the metathesis reaction to precipitate a gaseous desulfurization active agent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210443907.XA CN114534465B (en) | 2022-04-26 | 2022-04-26 | Flue gas calcium method desulfurization method and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210443907.XA CN114534465B (en) | 2022-04-26 | 2022-04-26 | Flue gas calcium method desulfurization method and device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114534465A true CN114534465A (en) | 2022-05-27 |
| CN114534465B CN114534465B (en) | 2022-10-28 |
Family
ID=81667536
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210443907.XA Active CN114534465B (en) | 2022-04-26 | 2022-04-26 | Flue gas calcium method desulfurization method and device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114534465B (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102485325A (en) * | 2011-04-19 | 2012-06-06 | 安徽理工大学 | Flue gas desulphurization technology with ammonium sulfate-calcium hydroxide slurry method |
| CN102658020A (en) * | 2012-05-24 | 2012-09-12 | 首钢总公司 | Ammonium-calcium dual-alkali flue gas desulfurization process |
-
2022
- 2022-04-26 CN CN202210443907.XA patent/CN114534465B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102485325A (en) * | 2011-04-19 | 2012-06-06 | 安徽理工大学 | Flue gas desulphurization technology with ammonium sulfate-calcium hydroxide slurry method |
| CN102658020A (en) * | 2012-05-24 | 2012-09-12 | 首钢总公司 | Ammonium-calcium dual-alkali flue gas desulfurization process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114534465B (en) | 2022-10-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101352647B (en) | Simultaneous desulfuration and denitration technique by wet flue gas method | |
| CN100488601C (en) | Flue gas desulfurization method by using magnesium compound and ammonia for circulated regeneration | |
| CN101607173B (en) | Desulfurization process of flue gas or waste gas by using external regenerative cycle magnesium sulfate method | |
| CN101352644A (en) | Wet flue gas denitration technique for nitrite recovery | |
| CN101428193A (en) | Wet-type desulfuration method for steel scoria with flue gas | |
| CN107281924A (en) | A kind of improved ammonia desulfurizing process and system | |
| CN103007718B (en) | Wet redox, desulfuration and resource utilization method for flue gas | |
| CN102284238A (en) | Bialkali-method flue-gas desulphurization process | |
| CN103585869A (en) | Flue gas purifying method with recyclable alkali absorption liquid | |
| CN102008880B (en) | Method for realizing integrated desulfurization and denitrification and product recovery based on magnesium-ammonium method | |
| CN102225307A (en) | Flue gas desulfurization process by using organic acid enhanced acetylene sludge | |
| KR0174794B1 (en) | Exhaust gas desulfurization process | |
| CN102441322A (en) | Method for desulfurizing flue gas and by-producing flocculant | |
| EP0097240B1 (en) | Process for removal of sulfur oxides from hot gases | |
| CN101480577A (en) | Desulfuration technique with jet bubble process using red mud as absorbing agent | |
| US5770164A (en) | Clear liquor organic acid flue gas desulfurization system | |
| US5486342A (en) | Clear liquor scrubbing of sulfur dioxide with forced oxidation in flue gas desulfurization system | |
| CN101829489A (en) | Ammonia-plaster mode desulphurization system | |
| CN109985497A (en) | The double section sulfur removal technologies of a kind of calcium, ammonia and equipment | |
| CN101898822A (en) | System and method for softening water for use in a scrubber | |
| CN109569222A (en) | The ammonia regeneration utilization process of the ammonia process of desulfurization | |
| CN114534465B (en) | Flue gas calcium method desulfurization method and device | |
| CN201791470U (en) | Dry-method suspension bed type flue gas desulfurization system for small and medium sized coal burning boiler | |
| CN105498503B (en) | A kind of dual alkali scrubbing FGD process method and flue gas desulphurization system | |
| CN102658020A (en) | Ammonium-calcium dual-alkali flue gas desulfurization process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |