CN107051171A - A kind of double tower magnesium method flue gas desulphurization technique - Google Patents
A kind of double tower magnesium method flue gas desulphurization technique Download PDFInfo
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- CN107051171A CN107051171A CN201710450003.9A CN201710450003A CN107051171A CN 107051171 A CN107051171 A CN 107051171A CN 201710450003 A CN201710450003 A CN 201710450003A CN 107051171 A CN107051171 A CN 107051171A
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- flue gas
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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
- B01D53/501—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
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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
- B01D53/501—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
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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
- C01F5/40—Magnesium sulfates
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Abstract
A kind of double tower magnesium method flue gas desulphurization technique, it includes a desulfurizing tower (2) and an oxidizing tower (10), and desulfurizing tower (2) uses magnesia magnesium sulfite desulfurization system；Oxidizing tower (10) uses the desulfurization of magnesia magnesium sulfate and oxidation system, former flue gas is divided into two parts, most of original flue gas introduces desulfurizing tower (2), fraction original flue gas introduces oxidizing tower (10), sulfur dioxide in fraction flue gas is by partial removal, and the magnesium sulfite in slurries, which is oxidized to after magnesium sulfate, discharges oxidizing tower.The present invention is advantageous in that：Relative to same magnesia magnesium sulfate sulfur removal technology, absorption system and oxidative system energy consumption of the invention reduces by more than 20%；The utilization rate of desulfurizing agent levels off to 100%, and the utilization rate of oxidation air close to 30% by bringing up to more than 38%.Although oxidizing tower need to additionally be set, because the flue gas used only accounts for the 2 25% of total former exhaust gas volumn, it is invested and operating cost is relatively low, and the integrated operation cost of desulphurization system still reduces by more than 15%.
Description
Technical field
The present invention relates to magnesium method flue gas desulphurization, more particularly, to magnesium method flue gas desulphurization technique and desulfurization product comprehensive utilization
The improvement of technique.
Background technology
Magnesium method flue gas desulphurization can be divided into magnesia-magnefite process and magnesium oxide-magnesium sulfate according to the difference of desulfurization product
Method, the former desulphurization system includes neutralisation unit and absorptive unit, is not provided with oxidation unit, its final desulfurization product as once takes off
Sulphur product-magnesium sulfite；The latter's desulphurization system includes absorbing, neutralizes, aoxidizes three reaction members, oxidation unit and neutralisation unit
In the same cavity of bottom of towe, once desulfurization product sulfurous acid (hydrogen) magnesium is magnesium sulfate in the air oxidation that bottom of towe is blasted, simultaneously
Part magnesium bisulfite is proceeded desulfurization and absorbed in (hydrogen) magnesia with generation magnesium sulfite.In desulfurization operation technological parameter
Aspect, magnesia-magnefite process absorbing liquid pH value is generally controlled in 6.0-6.5, with simultaneously take into account neutralization (pH it is more low more
It is good) and desulfurization absorb the requirement of (the higher the better by pH), it is 4-6L/m that it, which sprays liquid-gas ratio,3；And magnesium oxide-magnesium sulfate method, due to
Magnesium sulfite has higher solubility at a low ph, beneficial to the progress of oxidation reaction, therefore, the pH value of its absorbing liquid generally quilt
Control is below 6.0, accordingly, and it, which sprays liquid-gas ratio, need to reach 6-8L/m3The requirement of desulfurization absorption could be met.Therefore, after
It is higher than the former that the desulfurization of person absorbs energy consumption, in addition increased oxidation energy consumption, the desulfurization energy consumption of the latter than the former high 30% with
On.
Although magnesia-magnefite process has obvious power savings advantages relative to the sulfuric acid magnesium processes of magnesia one, it is passed
Desulfurization product comprehensive utilization mode (by the magnesium sulfite roasting heat recovery magnesia) investment of system is big, equipment corrosion is serious,
Cost recovery is high, and current common practice is by its landfill stabilization, it is impossible to implement comprehensive utilization.Followed simultaneously for desulfurization is departed from
The magnesium sulfite slurries of loop system, although its as reducing substances in theory can also oxidation by air, but in actual work
Be extremely hard to be oxidized in journey, this point turn into row in know together, but its origin cause of formation and be not known.Ground by substantial amounts of theoretical and experiment
Study carefully, we conclude that being：The magnesium sulfite slurries that magnesia-magnefite process is produced depart from after desulphurization circulating system, slurry
Liquid temperature drop, pH raise and are in alkaline (the usual desulfurizing agent excess 2-10% of desulphurization system), cause to be oxidized material sulfurous acid
Magnesium solubility is in the decline of the order of magnitude, in turn results in the gas-liquid mass transfer efficiency reduction that air forces oxidation, makes magnesium sulfite extremely difficult
It is oxidized, comprehensive utilization is reclaimed magnesium sulfate and is difficult to carry out.
Domestic Tsing-Hua University's National 863 project team reclaims the purpose of technical grade sulfuric acid magnesium based on low cost, has applied for multinomial
Magnesium processes desulfurization product reclaims the patent of sulfuric acid magnesium products.Although it has also recognized that magnesium sulfite slurries in desulphurization circulating system
The characteristics of being difficult to be oxidized outside, specify that in its granted patent (CN100335154C) " once depart from circulation, it is extremely difficult to aoxidize ",
But it does not study the origin cause of formation, does not propose solution pointedly with regard to this, its granted patent is caused without practicality.It authorizes special
Sharp CN100335154C《A kind of magnesium oxide flue gas desulfurization and product thick slurry process oxid-reclamatiom technique》Propose：Arranged using air oxidation
Go out the magnesium sulfite slurries of desulphurization system, and slurries external heat insulation (heating) is generated to prevent oxidation in oxidizing process
Magnesium sulfate crystallization, this measure objectively also serves lifting oxidation slurry temperature, improves and be oxidized material magnesium sulfite simultaneously
The effect of solubility, but it does not solve the pH value of solution rise problem bigger on oxidation reaction influence still, and oxidation mass-transfer efficiency is still
It is very low, while insulation steam need to be consumed.Based on generation high-concentration sulfuric acid magnesium solution, reduction subsequent sulphuric acid magnesium products crystallization energy consumption
Purpose, Tsing-Hua University another granted patent CN101530725B《A kind of wet magnesium oxide desulphurization product and automatic concentration reclaim work
Skill》Propose and concentration tower is set before desulfurizing tower, the magnesium sulfite slurries that desulfurization is generated enter with whole flue gases in concentration tower
Row gas-liquid mass transfer, and oxidative system oxidative magnesium slurries are set at concentration tower bottom.This method is solving desulfurization product concentration
While, the acidifying to magnesium sulfite slurries and insulation are objectively also achieved, oxidation mass-transfer efficiency is improved, but because it is adopted
Gas-liquid mass transfer is carried out with desulfurization product (magnesium sulfite slurries) in concentration tower with whole flue gases, concentration systems are in investment and energy
Desulphurization system has been even more than in terms of consumption.Therefore, above-mentioned two granted patents do not have actual successful application achievement.
The content of the invention：
In order to overcome the above-mentioned deficiencies of the prior art, the invention provides a kind of double tower magnesium method flue gas desulphurization technique, the work
Skill makes the desulfurization of most flue gases absorb anti-by the way of desulfurization absorptive unit and desulfurization product oxidation unit are separately positioned
It should be carried out in magnesia-magnesium sulfite desulfurization system that mass-transfer efficiency is high, energy consumption is low；Using a small amount of flue gas to magnesia-Asia
The desulfurization product magnesium sulfite slurries of magnesium sulfate desulfurization system are heated up, are acidified, and make oxidation reaction dense in higher reaction medium
Carried out under degree and reaction temperature, improve the utilization rate of oxygen, reduction oxidation energy consumption, while the desulfurization to a small amount of flue gas is realized, from
The problem of oxidation of the magnesium sulfite slurries of disengaging desulphurization circulating system system is fundamentally solved, while making excessive desulfurizing agent in oxidation
Reacted completely in tower, saved desulfurizing agent.
Technical solution of the present invention is as follows：
A kind of double tower magnesium method flue gas desulphurization technique, it includes a desulfurizing tower (2) and an oxidizing tower (10), desulfurizing tower
(2) magnesia-magnesium sulfite desulfurization system is used；Oxidizing tower (10) uses magnesium oxide-magnesium sulfate desulfurization and oxidation system, and it is wrapped
Include following steps：
Step 1, former flue gas is divided into two parts, most of original flue gas introduces the desulfurization for being not provided with desulfurization product oxidative system
Tower (2), the SO in gas-liquid mass transfer, removing flue gas is carried out using magnesium-based absorbing liquid and flue gas2, generate magnesium sulfite slurries；
Step 2, above-mentioned magnesium sulfite slurries are introduced into oxidizing tower (10), using the former flue gas of fraction and magnesium sulfite slurries
Gas-liquid mass transfer is carried out, magnesium sulfite slurries is heated up and/or is acidified, the sulfur dioxide in flue gas is by partial removal；
Step 3, to air is passed through in oxidizing tower (10), the magnesium sulfite in slurries be oxidized to discharge after magnesium sulfate aoxidized
Tower.
Above-mentioned double tower magnesium method flue gas desulphurization technique, described introduce magnesium sulfite slurries before oxidizing tower (10) removes it
In part moisture content, make the Adlerika concentration in discharge oxidizing tower slurries meet magnesium sulfate comprehensive utilization production requirement.
Typically in the steady area of crystallization medium of the concentration of the Adlerika of control oxidizing tower discharge at such a temperature, with most
Reduce to limits the crystallization energy consumption of subsequent sulphuric acid magnesium products.
Without (hydrogen) oxidation in above-mentioned double tower magnesium method flue gas desulphurization technique, the slurries of described discharge oxidizing tower (10)
Magnesium.
Above-mentioned double tower magnesium method flue gas desulphurization technique, the former flue gas of fraction described in step 2 accounts for the 2%- of total former flue gas
25%, preferably 2-10%.
Theoretically, as long as being passed through former flue gas in magnesium sulfite slurries, it necessarily leads to the effect of heating and/or acidifying
Really, oxidation mass-transfer efficiency also can be necessarily improved, the former exhaust gas volumn being passed through is bigger, and the pH of slurries is lower in desulfurizing tower, and temperature is got over
Height, the more raising beneficial to oxidation mass-transfer efficiency, but excessive former flue gas intake can cause oxidizing tower scale excessive, oxidation unit
Investment and operating cost improve, the reduction of the desulfuration efficiency of oxidizing tower.The flue gas intake of optimization is made into oxidizing tower sulfurous acid
(hydrogen) magnesia in magnesium slurries is fully neutralized reaction, magnesium sulfite slurries pH is less than 6.0.
Above-mentioned double tower magnesium method flue gas desulphurization technique, can one oxidizing tower (10) composition pair of many desulfurizing towers (2) configurations
Tower magnesium method flue gas desulphurization technique.
The present invention is advantageous in that：
For desulfurization angle：Relative to the magnesium oxide-magnesium sulfate sulfur removal technology equally by desulfurization product of magnesium sulfate, sheet
The absorption system and oxidative system energy consumption of invention reduce by more than 20%；The utilization rate of desulfurizing agent levels off to 100%, oxidation air
Utilization rate by bringing up to more than 38% close to 30%.Although oxidizing tower need to additionally be set, due to aoxidizing the former flue gas used
2%-25% of total former flue gas or so is only accounted for, it is invested and operating cost is relatively low, and the integrated operation cost of desulphurization system is still
Reduction by more than 15%.For magnesium sulfate comprehensive utilization angle：On the premise of using above-mentioned sulfur removal technology, by simply will
Magnesium sulfite dewatering slurries enter back into the means of oxidizing tower oxidation, and same concentration can be reached on the premise of a small amount of flue gas is used
Purpose, so that magnesium sulfate, which is reclaimed, possesses economic value.
For many set magnesium processes desulphurization systems, magnesia-magnefite process desulphurization system is implemented according to technical solution of the present invention
With the configuration of oxidizing tower (magnesium oxide-magnesium sulfate method desulphurization system), sulfurous acid can be solved while desulfurization operation cost is reduced
Magnesium Solid state fermentation problem.Simultaneously for the desulfurization system that smoke evaporative ability is relatively low or desulfurization product magnesium sulfite accounting is relatively low,
Purpose to Adlerika concentrate can also be reached using this technique.
Brief description of the drawings
Fig. 1 is process flow diagram of the invention.
A kind of double tower flue gas desulfurization process figure for conventional flue gas that Fig. 2 provides for the present invention.
A kind of double tower flue gas desulfurization process figure for low-temperature flue gas that Fig. 3 provides for the present invention.
Fig. 4 covers a kind of double tower flue gas desulfurization process figure associated with desulphurization systems more for what the present invention was provided for.
Wherein：1 is former flue gases duct, and 2 be desulfurizing tower, and 3 be desulfurizing tower bottom of towe liquid storage section, and 4 be desulfurizing tower spraying layer, and 5 are
Demister, 6 be Wet chimney, and 7 be solid-liquid separator, and 8 be precooling spray before desulfurizing tower tower, and 9 be magnesia material-compound tank, and 10 be oxygen
Change tower, 11 be oxidizing tower bottom of towe liquid storage section, and 12 be oxidizing tower spraying layer, and 13 be oxidation fan, and 14 be precooling before oxidizing tower tower
Spray, 15 be branch road flue.
Embodiment
As shown in process chart Fig. 1：Most of former flue gas by dust removal process enters desulfurization system through former flue gases duct 1
System, sends into desulfurizing tower 2, the desulphurization circulating sprayed with desulfurizing tower spraying layer 4 after 8 spraying coolings of spray are precooled before desulfurizing tower tower
Slurries counter current contacting absorbs SO2, emptied after the demisting of demister 5 through tower top Wet chimney 6, desulfurizing tower bottom of towe liquid storage section 3 is not set
Put desulfurization product oxidative system.As the magnesia powder of desulfurizing agent, carried out in magnesia preparing tank 9 with slurry, magnesia slurry enters
Enter desulfurizing tower 2 and carry out circulated sprinkling absorption.Partial desulfurization loop slurry enters solid-liquid separator 7, and solid-liquid separator underflow is introduced
Oxidizing tower 10, dilute phase solution, which is pumped into before desulfurizing tower tower to precool, precools the former flue gas of 14 pairs of spray before spray 8 and/or oxidizing tower tower
Cool down.Meanwhile, the former flue gas of fraction by dust removal process enters desulfurization product oxidative system through branch road flue 15,
Enter oxidizing tower 10 after 14 spraying coolings of spray are precooled before oxidized tower tower, the loop slurry sprayed with oxidizing tower spraying layer 12
Gas-liquid mass transfer, is heated up and/or is acidified, and excessive (hydrogen) magnesia is neutralized.From oxidation fan 13 to oxidizing tower bottom liquid storage
Section 11 blasts oxidation air, aoxidizes sulfurous acid (hydrogen) magnesium therein, completes to arrange or comprehensively utilize back outside the Adlerika of oxidation
Receive magnesium sulfate.The former flue gas of fraction for completing gas-liquid mass transfer goes out the SO of oxidizing tower depending on it2Concentration, compares the environment protection emission that need to be performed
Standard, may be selected direct qualified discharge, mixed with desulfurizing tower neat stress after qualified discharge, enter row up to standard after desulfurizing tower advanced treating
Put.
By above-mentioned technological process, we implement desulfurization and desulfurization product to three different types of flue gases of different industries
Oxidation, detail parameters are shown in embodiment.
The conventional flue gas double tower flue gas desulfurization of embodiment 1. (being discharged after mixing)
Certain enterprise Industrial Boiler operating mode exhaust gas volumn 300000m3/ h, SO2Concentration is 1800mg/m3, cigarette temperature is 145 DEG C.By upper
The technological process for stating invention sets desulfurizing tower (2) diameter 6600mm, high 18000mm；Oxidizing tower (10) diameter 1000mm is high
12000mm, desulfurizing tower (2) desulfuration efficiency is up to 97.75%, desulfurizing tower (2) outlet SO2Concentration is only 32.6mg/m3.Using 2%
Former flue gas in the oxidizing tower (10) with after loop slurry counter current contacting, SO2Concentration drops to 130.5mg/m3, oxidizing tower (10)
Entoplasm liquid magnesium sulfate concentration is 33.2%, and oxidation air coefficient of oxygen utilization reaches 42.6%.Oxidizing tower (10) exiting flue gas is introduced
In desulfurizing tower (2) chimney flue gas dual disposal, mixed flue gas SO are discharged with desulfurizing tower2Concentration remains to meet《GB13271-
2014 emission standard of air pollutants for boilers》Requirement.
The low-temperature flue gas of embodiment 2. (secondary desulfuration)
The coloured kiln operating mode exhaust gas volumn of certain enterprise is 350000m3/ h, SO2Concentration is 2200mg/m3, cigarette temperature is 45 DEG C.Press
The technological process of foregoing invention sets desulfurizing tower (2) diameter 7000mm, high 18000mm；Oxidizing tower (10) diameter 3600mm is high
15000mm.Relatively low cigarette temperature makes before desulfurizing tower without setting the part dilute phase solution precooled in spray system, solid-liquid separator
Part is outer to arrange.25% former flue gas salification cycles slurries are passed through in oxidizing tower (10), magnesium sulfite oxidation rate is improved, realizes
Slurries concentrate, its magnesium sulfate concentration has reached 27.6%, successfully solves slurries concentrate of the flue gas without evaporability desulphurization system
Problem.Oxidation air coefficient of oxygen utilization reaches 42.3%.Oxidizing tower (10) exports SO2Concentration is 427mg/m3, flue gas introducing desulfurizing tower
(2) qualified discharge after secondary desulfuration is carried out in.The successful implementation explanation of the present embodiment present invention can be suitably applied to the row such as coloured, chemical industry
Desulphurization system largely generates the high oxygen gas and sulfuric-acid production tail gas of magnesium sulfate, and some low temperature (40-80 DEG C) nothings in industry
The flue gas of evaporability.
The combination (directly discharging) of the set desulphurization system of embodiment more than 3.
There are 12 boilers in certain factory, and operating mode exhaust gas volumn is 100000m3/ h, SO2Concentration is 1260mg/m3, cigarette temperature is 135
℃.Wherein 11 boiler flue gas desulfurizations use magnesia-magnefite process desulphurization system, and 1 boiler smoke is passed through oxidizing tower (oxygen
Change magnesium-sulfuric acid magnesium processes desulphurization system) desulfurization is carried out, and the magnesium sulfite slurries produced using above-mentioned 11 boiler desulfurizations are as de-
Sulphur agent, as shown in Figure 4.Oxidizing tower (10) exports SO2Concentration is 42mg/m3, met《GB13223-2011 thermal power plants air
Pollutant emission standard》In requirement, can directly discharge.It is 34.6%, oxidation air oxygen to go out oxidizing tower slurries magnesium sulfate concentration
Utilization rate reaches 38.3%.
Claims (6)
1. a kind of double tower magnesium method flue gas desulphurization technique, it is characterized in that：It includes a desulfurizing tower (2) and an oxidizing tower (10),
Desulfurizing tower (2) uses magnesia-magnesium sulfite desulfurization system；Oxidizing tower (10) uses magnesium oxide-magnesium sulfate desulfurization and oxysome
System, it comprises the following steps：
Step 1, former flue gas is divided into two parts, most of original flue gas introduces the desulfurizing tower for being not provided with desulfurization product oxidative system
(2) SO in gas-liquid mass transfer, removing flue gas, is carried out using magnesium-based absorbing liquid and flue gas2, generate magnesium sulfite slurries；
Step 2, above-mentioned magnesium sulfite slurries are introduced into oxidizing tower (10), carried out using the former flue gas of fraction and magnesium sulfite slurries
Gas-liquid mass transfer, makes magnesium sulfite slurries heat up and/or be acidified, the sulfur dioxide in flue gas is by partial removal；
Step 3, to air is passed through in oxidizing tower (10), the magnesium sulfite in slurries is oxidized to after magnesium sulfate and discharges oxidizing tower.
2. double tower magnesium method flue gas desulphurization technique according to claim 1, it is characterized in that：Described draws magnesium sulfite slurries
Enter removing part moisture content therein before oxidizing tower (10), the Adlerika concentration in discharge oxidizing tower slurries is met magnesium sulfate
Comprehensively utilize the requirement of production.
3. double tower magnesium method flue gas desulphurization technique according to claim 1, it is characterized in that：Described discharge oxidizing tower (10)
(hydrogen) magnesia is free of in slurries.
4. double tower magnesium method flue gas desulphurization technique according to claim 1, it is characterized in that：The former cigarette of fraction described in step 2
Gas accounts for the 2%-25% of total former flue gas.
5. double tower magnesium method flue gas desulphurization technique according to claim 4, it is characterized in that：The former cigarette of fraction described in step 2
Gas accounts for the 2%-10% of total former flue gas.
6. double tower magnesium method flue gas desulphurization technique according to claim 1, it is characterized in that：Many desulfurizing towers (2) configure one
Oxidizing tower (10) constitutes double tower magnesium method flue gas desulphurization technique.
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| CN2017103330399 | 2017-05-12 | ||
| CN201710333039 | 2017-05-12 |
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| CN107051171A true CN107051171A (en) | 2017-08-18 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109422284A (en) * | 2017-08-24 | 2019-03-05 | 程相魁 | The integrated processes of flue gas desulfurization and the pollutant resources treatment of wastes with processes of wastes against one another of combustion gas deamination |
| CN110790290A (en) * | 2019-12-18 | 2020-02-14 | 河南省睿博环境工程技术有限公司 | Method for producing high-purity magnesium sulfate from magnesium-method desulfurization waste residues |
| CN114768498A (en) * | 2022-05-05 | 2022-07-22 | 重庆远达烟气治理特许经营有限公司科技分公司 | Magnesium desulfurization system and method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101549245A (en) * | 2008-04-03 | 2009-10-07 | 上海瑞惠机械设备制造有限公司 | Desulfurizing method of spraying flue gas purifier for flue gas desulfurization of sintering machines |
| CN105013317A (en) * | 2015-07-03 | 2015-11-04 | 赵亮 | Process flow for recovering high-purity magnesium sulfite by magnesium oxide flue gas desulphurization |
-
2017
- 2017-06-14 CN CN201710450003.9A patent/CN107051171A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101549245A (en) * | 2008-04-03 | 2009-10-07 | 上海瑞惠机械设备制造有限公司 | Desulfurizing method of spraying flue gas purifier for flue gas desulfurization of sintering machines |
| CN105013317A (en) * | 2015-07-03 | 2015-11-04 | 赵亮 | Process flow for recovering high-purity magnesium sulfite by magnesium oxide flue gas desulphurization |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109422284A (en) * | 2017-08-24 | 2019-03-05 | 程相魁 | The integrated processes of flue gas desulfurization and the pollutant resources treatment of wastes with processes of wastes against one another of combustion gas deamination |
| CN110790290A (en) * | 2019-12-18 | 2020-02-14 | 河南省睿博环境工程技术有限公司 | Method for producing high-purity magnesium sulfate from magnesium-method desulfurization waste residues |
| CN114768498A (en) * | 2022-05-05 | 2022-07-22 | 重庆远达烟气治理特许经营有限公司科技分公司 | Magnesium desulfurization system and method |
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