CN103551015A - Sulfur dioxide absorbent prepared from two-alkali salt slurry - Google Patents
Sulfur dioxide absorbent prepared from two-alkali salt slurry Download PDFInfo
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Abstract
The invention discloses a sulfur dioxide absorbent prepared from a two-alkali salt slurry. A preparation method of the absorbent comprises the following steps: washing the two-alkali salt slurry with water, adding water to a slurry having a solid content of 5-30%, adding an organic acid additive having a mass being 0.05-1% of the mass of the salt slurry to the obtained slurry, and uniformly mixing. In the invention, limestone powder is substituted by the processed two-alkali salt slurry, thereby multiple purposes comprising the change of wastes to wastes, the change of wastes to valuables, energy saving, emission reduction desulphurization cost reduction and the like are realized.
Description
Technical field
The present invention relates to wet desulphurization aspect, be specifically related to a kind of sulfur dioxide absorbent that two alkaline process salt slurries are raw material of take, belong to field of environment protection and solid waste resource recovery utilizes technical field.
Background technology
Bittern purifying, also referred to as the pretreatment of bittern, is one of critical process in salt producing craft process, and object is by the Ca in former halogen
2+, Mg
2+ion is separated before entering heating clamber.Salt slurry, is the general name of the various inorganic salts of discharging in this process.
Two alkaline process bittern purifyings are to utilize caustic soda (NaOH) by the Mg in bittern
2+, with Mg (OH)
2precipitation is removed, and utilizes soda ash (NaCO
3) by the Ca in bittern
2+with CaCO
3precipitation form is removed.The fundamental reaction formula of two alkaline process is as follows:
2OH
-+Mg
2+→Mg(OH)
2↓
Ca
2++CO
3 2-→CaCO
3↓
Two alkaline process salt slurry main components are CaCO
3, also contain in addition a small amount of NaCl, CaSO
4and Mg (OH)
2.If can not only solve the processing problem of two alkaline process salt slurries by two alkaline process salt slurries for desulfuration field, also can greatly reduce desulphurization cost, obtain good Social benefit and economic benefit.
Present stage, the desulfurization program that mainly adopts of power plants was wet desulphurization, and principle is as follows: flue gas enters the wet-type absorption tower of desulfurizer, with the caustic lime stone slurries droplet counter current contacting of spray from top to bottom, and acidic oxide SO wherein
2and other pollutants HCl, HF etc. are absorbed, flue gas is able to abundant purification; Absorb SO
2after slurry reaction generate CaSO
3, by forced oxidation, crystallization generate CaSO on the spot
42H
2o obtains commerical grade desulfuration byproduct-gypsum after dehydration, finally realizes the comprehensive regulation of sulfur-containing smoke gas.The main reaction course of limestone-gypsum method Wet Flue Gas Desulfurization Technique is as follows:
1, absorb
SO
2+H
2O→H
2SO
3
2, neutralization
CaCO
3+H
2SO
3→CaSO
3+CO
2↑+H
2O
3, oxidation
2CaSO
3+O
2→2CaSO
4↓。
Application number 200710151361.6 discloses a kind of sulphur dioxide salty mud absorbent.In this patent, the salt slurry of use is the waste residue salt slurry that desalinization of soil by flooding or leaching program in soda ash production process in chlorine industry produces, and after directly sizing mixing, carries out flue gas desulfurization.The non-two alkaline process salt slurries of salt slurry that this method is used, and salt slurry is without further processing, does not use additive, desulfurization degree >=95.Because the method the processing such as does not wash to salt slurry, in salt slurry, sodium chloride content is higher, on the one hand can etching apparatus, reduce on the other hand reaction rate; In addition salt slurry dissolves and SO
2reaction speed is slow, so lime stone conversion rate is slower in the method salt slurry, is difficult to reach the desulfurized effect of agstone.
Application number 201210565053.9 discloses the application of a kind of filter mud of sugar refinery in smoke-gas wet desulfurization.In this patent, use be filter mud of sugar refinery as desulfurizing agent for limestone-gypsum method wet desulphurization, desulfurization degree >=95; And the physico-chemical property to filter mud of sugar refinery is analyzed, calcium carbonate content >=90.What the method was used is that filter mud of sugar refinery carries out desulfurization, is also the comprehensive utilization of solid waste.But in the method, the simple filter mud that uses carries out desulfurization, and its actual desulfurized effect does not surpass agstone.
Summary of the invention
The object of this invention is to provide a kind of sulfur dioxide absorbent being applied in heat-engine plant wet desulfurization, utilize two alkaline process salt slurries to substitute after treatment agstone above, realize waste recycling, turn waste into wealth, the multiple target such as energy-saving and emission-reduction, reduction desulfurization expense.
Object of the present invention can reach by following measures:
A kind ofly take the sulfur dioxide absorbent that two alkaline process salt slurries are raw material, this absorbent makes by the following method: after two alkaline process salt slurry washings, add water move to solid content and be 5～30% slurries, then to the organic additive that adds salt slurry quality 0.05～1% in slurries, mix and get final product.
Primary raw material two alkaline process salt slurry, wherein CaCO in this absorbent
3content is 80～92%, and its grain diameter is 20～80 μ m; Preferably, CaCO in two alkaline process salt slurries
3content is also to contain NaCl, CaSO in 85～90%, two alkaline process salt slurries
4and Mg (OH)
2, its grain diameter is 30～50 μ m.
Water-washing step in the present invention is specially: by two alkaline process salt slurries and the water ratio mixing, washing of 1:1～3 in mass ratio, and repeated washing 0～3 time again after washing, dehydration after washing.The repetition here refers to not repeated washing (only washing 1 time) for 0 time.The lifting of washing times is conducive to improve the effect of final absorbent.Dehydration after washing can adopt reduced vacuum dehydration, as the dehydration of concrete employing vacuum-type drum filter etc.Wash and dewater after salt slurry need reach following standard: in the salt slurry after washing, CaCO
3contents on dry basis 90～97%, preferably more than 94% and be less than 97%, NaCl contents on dry basis < 1%, grain diameter 20～80 μ m.
After two alkaline process salt slurries washings, add water adjust the solid content of slurries be preferably 10～20%.
The organic additive of stating in the present invention is selected from one or more in citric acid, hexanedioic acid or acetic acid, and wherein citric acid purity is more than 97%, and hexanedioic acid purity is more than 97%, and acetic acid purity is more than 97%; The addition of the organic additive that slurries add is preferably into salt slurry dry weight 0.1～0.3%.By using organic additive, can promote the dissolving of lime stone, improve the utilization rate of absorbent; The pH value of simultaneous buffering absorption liquid, suppresses on gas-liquid interface due to SO
2the reduction of the pH value of dissolving and causing, has accelerated SO
2absorption, thereby improve desulfuration efficiency, reduce operating cost.In organic acid and salt slurry, the interaction of other materials can further improve from chemical and physics aspect the desulfurized effect of salt slurry in addition.
The invention also discloses a kind of preparation method of take the sulfur dioxide absorbent that two alkaline process salt slurries are raw material: by two alkaline process salt slurries after washing, add water move to solid content and be 5～30% slurries, to the organic additive that adds salt slurry quality 0.05～1% in slurries, mix and get final product again; Wherein said organic additive is selected from one or more in citric acid, hexanedioic acid or acetic acid.Each process in preparation method and optimum condition are as mentioned above.
After sulfur dioxide absorbent of the present invention prepares, can directly apply in wet desulphurization equipment, be specially the absorbent preparing is sprayed from top to bottom in desulfurizing tower, and flue gas from bottom to top with slurries convection current, the same calcium carbonate reaction of sulfur dioxide in this process, produce calcium sulfite solution, flue gas after treatment reaches discharge standard.Then calcium sulfite solution is further oxidized to calcium sulfate, then dehydration obtains desulfurated plaster, and whole process finishes.A whole set of desulfurizer generally can be divided into flue gas system, slurries system, desulfurizing adsorption system, fresh water (FW) system, emptying system, this six large system of gypsum dehydration system, and concrete equipment can be directly with reference to existing wet desulphurization equipment.
In above-mentioned application, two alkaline process salt slurries remove sulfur dioxide after simple process is made into desulfurization absorbent, calcium carbonate in sulfur dioxide and salt slurry generates gypsum, other is identical with limestone-gypsum method wet desulphurization method, therefore should " wet desulphurization that two alkaline process salt slurries are absorbent " method can be referred to as " two alkaline process salt slurry-gypsums " wet desulphurization.
Beneficial effect of the present invention:
It is primary raw material that two alkaline process salt slurries are directly take in the present invention, through salt slurry simple process, and by using additive, improve desulfuration efficiency, reduced desulphurization cost in " two alkaline process salt slurry-gypsums " of the present invention, added after additive in slurries, assimilation effect is increased dramatically: CaCO in salt slurry
3transform mark and reach 0.8 o'clock required time at 50～100min, reaction rate is better than granularity 325 orders, CaCO
3content 95% agstone.For absorbing the sulfur dioxide (S0 of flue gas
2), be applied to circulating fluidized bed desulfur, S0
2clearance reach more than 96%.
It is wet desulphurization absorbent that salt making enterprises two alkaline process salt slurries are take in the present invention, desulfuration efficiency is high, meet national desulfurization standard, this method is directly used two alkaline process salt slurries, need not further to salt slurry, dry, calcination process, simplify technique, reduce energy consumption, in addition, two alkaline process salt slurries are as enterprise's waste residue, draw materials convenient economical, processing procedure is simple, general to the requirement of equipment and Limestone-gypsum Wet Flue Gas Desulfurization Process, both saved the expense of buying desulfurizing agent, outlet has been found in the safe disposal that is again two alkaline process salt slurries, solve salt making enterprises solid waste and process problem, realized waste recycling, the target of energy-saving and emission-reduction.There is larger Social benefit and economic benefit.
The specific embodiment
Below by instantiation, the present invention is described further, and following explanation is only to play explanation effect, its content is not limited.
The present invention's " two application of alkaline process salt slurry in heat-engine plant wet desulfurization " is except absorbent difference, consistent with the technology of limestone-gypsum method wet desulphurization now.Technological process is roughly: by two alkaline process salt slurry operating weights, than after being the washing 1～3 time of 1～3 times, being mixed to form solid content with water is 10～20% slurries, then adds the additive of salt slurry dry weight 0.1～0.3%, and absorbent slurry has configured; By deduster flue gas out, by desulfurization blower fan, introduce desulphurization system, salt slurry slurries are delivered to spraying layer from slurry pool of absorption tower, the nozzle atomization of slurries on spraying layer becomes the droplet of certain diameter, in the process that droplet falls with absorption tower in the flue gas counter current contacting that rises, droplet is removed the sulfur dioxide component of flue gas, S0
2clearance reach more than 96%.Clean flue gas is directly discharged through chimney, and the oxidation of the calcium sulfite of the generation force air that oxidized blower fan blasts in the circulation stock tank of bottom, absorption tower, finally generates gypsum, by gypsum pump, is discharged, and sends into gypsum dehydration system.
Each main component of the two alkaline process salt slurries that embodiment adopts: CaCO
3: 86.9%, NaCl:5.4%, CaSO
4: 5.2%, Mg (OH)
2: 2.5%.By the analysis to salt slurry particle diameter, the average grain diameter of salt slurry is 40 μ m.
Calcium carbonate activity test method in slurries: measure 250mL0.1mol/L CaCl with graduated cylinder
2solution, injects beaker, and it is placed in water-bath, controls temperature 50 C and makes after its constant temperature, with electronic balance, takes 0.15 salt slurry (doing), adds in the beaker of constant temperature, and inserts the paddle of agitator, and speed is 800r/min, continuous stirring 5min.
PH meter electrode is inserted in suspension to be measured, and attention electrode is not encountered paddle.It is 5.5 that autotitrator is set pH value, with 0.1mol/L hydrochloric acid solution, starts titration, and the table that simultaneously clocks starts to clock, and records not the hydrochloric acid solution consumption of t in the same time.This experiment in triplicate.
In sample, in salt slurry, lime stone transforms formula (1) calculating for mark:
In formula:
Constantly, in salt slurry, the conversion mark of lime stone, gets 0.8 to X (t): t;
C
hCl: the concentration of hydrochloric acid is 0.0lmol/L;
V
hCI(t): the t moment, the hydrochloric acid volume that titration consumes, mL;
W: the quality of the salt slurry taking is 0.150g;
W
(CaCO3): the quality percentage of calcium carbonate in salt slurry is measured value;
M
(CaCO3): the molecular weight of calcium carbonate is 100;
The volume of required titration hydrochloric acid when lime stone conversion mark is 0.8 in salt slurry according to formula (1) calculating.Measure lime stone and transform mark and reached for 0.8 required time, using now between as the index of sign salt slurry reaction rate.
Embodiment 1
Get two alkaline process salt slurries, the water washing of use identical weight 1 time, is used vacuum-type drum filter dehydration, CaCO in butt
3content is that 94.8, NaCl content is 0.97.The slurries that preparation solid content is 15%, then add salt slurry butt gross weight 0.1 citric acid (purity >=97%), and fully mix and blend, makes desulfurization absorbent slurries.
Use People's Republic of China's power industry standard (the mensuration > > DL/T943-2005 of agstone reaction rate for < < smoke-gas wet desulfurization), calcium carbonate activity in the slurries that make is tested.Test result shows, calcium carbonate conversion ratio is 0.8 o'clock, and the time of consumption is 60min.
The flue gas that 3 75t/h CFBBs of Dui Mou steam power plant produce carries out desulfurization, and flue-gas temperature is controlled at 145 ℃, flow-control 380000m
3/ h, stablizes after 2h, SO in flue gas
2concentration is 2690mg/Nm
3.By using after this slurries desulfurization, SO
2concentration is down to 91mg/Nm
3, desulfuration efficiency η=96.6%.
Embodiment 2
Get two alkaline process salt slurries, with the water washing of 2 times of weight 1 time, use vacuum-type drum filter dehydration, CaCO in butt
3content is that 96.4, NaCl content is 0.84.The slurries that preparation solid content is 10%, then add salt slurry butt gross weight 0.2 citric acid (purity >=97%), and fully mix and blend, makes desulfurization absorbent slurries.
Use People's Republic of China's power industry standard (the mensuration > > DL/T943-2005 of agstone reaction rate for < < smoke-gas wet desulfurization), calcium carbonate activity in the slurries that make is tested.Test result shows, calcium carbonate conversion ratio is 0.8 o'clock, and the time of consumption is 56min.
The flue gas that 3 75t/h CFBBs of Dui Mou steam power plant produce carries out desulfurization, and flue-gas temperature is controlled at 145 ℃, flow-control 380000m
3/ h, stablizes after 2h, SO in flue gas
2concentration is 2745mg/Nm
3.By using after this slurries desulfurization, SO
2concentration is down to 82mg/Nm
3, desulfuration efficiency η=97.0%.
Embodiment 3
Get two alkaline process salt slurries, the water washing of use identical weight 2 times, is used vacuum-type drum filter dehydration, CaCO in butt
3content is that 96.8, NaCl content is 0.81.The slurries that preparation solid content is 15%, then add salt slurry butt gross weight 0.2 citric acid (purity >=97%), and fully mix and blend, makes desulfurization absorbent slurries.
Use People's Republic of China's power industry standard (the mensuration > > DL/T943-2005 of agstone reaction rate for < < smoke-gas wet desulfurization), calcium carbonate activity in the slurries that make is tested.Test result shows, calcium carbonate conversion ratio is 0.8 o'clock, and the time of consumption is 49min.
The flue gas that 3 75t/h CFBBs of Dui Mou steam power plant produce carries out desulfurization, and flue-gas temperature is controlled at 145 ℃, flow-control 380000m
3/ h, stablizes after 2h, SO in flue gas
2concentration is 2638mg/Nm
3.By using after this slurries desulfurization, SO
2concentration is down to 24mg/Nm
3, desulfuration efficiency η=99.1%.
Embodiment 4
Get two alkaline process salt slurries, the water washing of use identical weight 3 times, is used vacuum-type drum filter dehydration, CaCO in butt
3content is that 96.8, NaCl content is 0.76.The slurries that preparation solid content is 15%, then add salt slurry butt gross weight 0.2 acetic acid (purity >=97%), and fully mix and blend, makes desulfurization absorbent slurries.
Use People's Republic of China's power industry standard (the mensuration > > DL/T943-2005 of agstone reaction rate for < < smoke-gas wet desulfurization), calcium carbonate activity in the slurries that make is tested.Test result shows, calcium carbonate conversion ratio is 0.8 o'clock, and the time of consumption is 59min.
The flue gas that 3 75t/h CFBBs of Dui Mou steam power plant produce carries out desulfurization, and flue-gas temperature is controlled at 145 ℃, flow-control 380000m
3/ h, stablizes after 2h, SO in flue gas
2concentration is 2627mg/Nm
3.By using after this slurries desulfurization, SO
2concentration is down to 102mg/Nm
3, desulfuration efficiency η=96.1%.
Embodiment 5
Get two alkaline process salt slurries, with the water washing of 2 times of weight 3 times, use vacuum-type drum filter dehydration, CaCO in butt
3content is that 96.9, NaCl content is 0.75.The slurries that preparation solid content is 15%, then add salt slurry butt gross weight 0.2 adipic acid (purity >=97%), and fully mix and blend, makes desulfurization absorbent slurries.
Use People's Republic of China's power industry standard (the mensuration > > DL/T943-2005 of agstone reaction rate for < < smoke-gas wet desulfurization), calcium carbonate activity in the slurries that make is tested.Test result shows, calcium carbonate conversion ratio is 0.8 o'clock, and the time of consumption is 57min.
The flue gas that 3 75t/h CFBBs of Dui Mou steam power plant produce carries out desulfurization, and flue-gas temperature is controlled at 145 ℃, flow-control 380000m
3/ h, stablizes after 2h, SO in flue gas
2concentration is 2611mg/Nm
3.By using after this slurries desulfurization, SO
2concentration is down to 84mg/Nm
3, desulfuration efficiency η=96.8%.
Embodiment 6
Get two alkaline process salt slurries, the water washing of use identical weight 2 times, is used vacuum-type drum filter dehydration, CaCO in butt
3content is that 96.4, NaCl content is 0.84.The slurries that preparation solid content is 20%, then add salt slurry butt gross weight 0.2 citric acid (purity >=97%), and fully mix and blend, makes desulfurization absorbent slurries.
Use People's Republic of China's power industry standard (the mensuration > > DL/T943-2005 of agstone reaction rate for < < smoke-gas wet desulfurization), calcium carbonate activity in the slurries that make is tested.Test result shows, calcium carbonate conversion ratio is 0.8 o'clock, and the time of consumption is 48min.
The flue gas that 3 75t/h CFBBs of Dui Mou steam power plant produce carries out desulfurization, and flue-gas temperature is controlled at 145 ℃, flow-control 380000m
3/ h, stablizes after 2h, SO in flue gas
2concentration is 2758mg/Nm
3.By using after this slurries desulfurization, SO
2concentration is down to 27mg/Nm
3, desulfuration efficiency η=99.0%.
Comparative example 1
Get two alkaline process salt slurries, the water washing of use identical weight 2 times, is used vacuum-type drum filter dehydration, CaCO in butt
3content is that 96.4, NaCl content is 0.84.The slurries that preparation solid content is 20%, do not add additive, directly make desulfurization absorbent slurries.
Use People's Republic of China's power industry standard (the mensuration > > DL/T943-2005 of agstone reaction rate for < < smoke-gas wet desulfurization), calcium carbonate activity in the slurries that make is tested.Test result shows, calcium carbonate conversion ratio is 0.8 o'clock, and the time of consumption is 78min.
The flue gas that 3 75t/h CFBBs of Dui Mou steam power plant produce carries out desulfurization, and flue-gas temperature is controlled at 145 ℃, flow-control 380000m
3/ h, stablizes after 2h, SO in flue gas
2concentration is 2749mg/Nm
3.By using after this slurries desulfurization, SO
2concentration is down to 297mg/Nm
3, desulfuration efficiency η=89.2%.
Comparative example 2
By agstone (CaCO
3content is 95.1%, and granularity is 325 orders) not doping, directly prepare solid content and be 20% desulfurization and absorb slurries.
Use People's Republic of China's power industry standard (the mensuration > > DL/T943-2005 of agstone reaction rate for < < smoke-gas wet desulfurization), calcium carbonate activity in the slurries that make is tested.Test result shows, calcium carbonate conversion ratio is 0.8 o'clock, and the time of consumption is 65min.
The flue gas that 3 75t/h CFBBs of Dui Mou steam power plant produce carries out desulfurization, and flue-gas temperature is controlled at 145 ℃, flow-control 380000m
3/ h, stablizes after 2h, SO in flue gas
2concentration is 2673mg/Nm
3.By using after this slurries desulfurization, SO
2concentration is down to 150mg/Nm
3, desulfuration efficiency η=94.4%.
Comparative example 3
By agstone (CaCO
3content is 95.1%, and granularity is 325 orders), directly prepare solid content and be 20% slurries, add agstone butt gross weight 0.2% citric acid (purity>=97%), abundant mix and blend, desulfurization absorbs slurries.
Use People's Republic of China's power industry standard (the mensuration > > DL/T943-2005 of agstone reaction rate for < < smoke-gas wet desulfurization), calcium carbonate activity in the slurries that make is tested.Test result shows, calcium carbonate conversion ratio is 0.8 o'clock, and the time of consumption is 61min.
The flue gas that 3 75t/h CFBBs of Dui Mou steam power plant produce carries out desulfurization, and flue-gas temperature is controlled at 145 ℃, flow-control 380000m
3/ h, stablizes after 2h, SO in flue gas
2concentration is 2673mg/Nm
3.By using after this slurries desulfurization, SO
2concentration is down to 118mg/Nm
3, desulfuration efficiency η=95.6%.
Claims (10)
1. take the sulfur dioxide absorbent that two alkaline process salt slurries are raw material for one kind, it is characterized in that this absorbent makes by the following method: after two alkaline process salt slurry washings, add water move to solid content and be 5～30% slurries, to the organic additive that adds salt slurry quality 0.05～1% in slurries, mix and get final product again.
2. according to claim 1ly take the sulfur dioxide absorbent that two alkaline process salt slurries are raw material, it is characterized in that CaCO in described two alkaline process salt slurries
3content is 80～92%, and its grain diameter is 20～80 μ m; Preferably, CaCO in two alkaline process salt slurries
3content is also to contain NaCl, CaSO in 85～90%, two alkaline process salt slurries
4and Mg (OH)
2, its grain diameter is 30～50 μ m.
3. according to claim 1ly take the sulfur dioxide absorbent that two alkaline process salt slurries are raw material, it is characterized in that described water-washing step is: by two alkaline process salt slurries and the water ratio mixing, washing of 1:1～3 in mass ratio, repeated washing 0～3 time again after washing, dehydration after washing.
4. according to claim 1ly take the sulfur dioxide absorbent that two alkaline process salt slurries are raw material, it is characterized in that in the salt slurry after washing CaCO
3contents on dry basis 90～97%, preferably more than 94% and be less than 97%, NaCl contents on dry basis < 1%, grain diameter 20～80 μ m.
5. according to claim 1ly take the sulfur dioxide absorbent that two alkaline process salt slurries are raw material, it is characterized in that adding after described two alkaline process salt slurries washings water adjust the solid content of slurries be 10～20%.
6. according to claim 1ly take the sulfur dioxide absorbent that two alkaline process salt slurries are raw material, it is characterized in that described organic additive is selected from one or more in citric acid, hexanedioic acid or acetic acid.
7. according to the sulfur dioxide absorbent that two alkaline process salt slurries are raw material of take described in claim 1 or 6, the amount that it is characterized in that the organic additive that described slurries add is 0.1～0.3% of salt slurry quality.
8. take the preparation method of the sulfur dioxide absorbent that two alkaline process salt slurries are raw material for one kind, it is characterized in that two alkaline process salt slurries after washing, add water move to solid content and be 5～30% slurries, then to the organic additive that adds salt slurry quality 0.05～1% in slurries, mix and get final product; Wherein said organic additive is selected from one or more in citric acid, hexanedioic acid or acetic acid.
9. method according to claim 8, is characterized in that CaCO in described two alkaline process salt slurries
3content is 80～92%, and its grain diameter is 20～80 μ m; Preferably, CaCO in two alkaline process salt slurries
3content is also to contain NaCl, CaSO in 85～90%, two alkaline process salt slurries
4and Mg (OH)
2, its grain diameter is 30～50 μ m; In salt slurry after washing, CaCO
3contents on dry basis 90～97%, preferably more than 94% and be less than 97%, NaCl contents on dry basis < 1%, grain diameter 20～80 μ m.
10. method according to claim 8, is characterized in that described water-washing step is: by lime-flue gas method secondary salt slurry and the water ratio mixing, washing of 1:1～3 in mass ratio, repeated washing 0～3 time, dehydration after washing; The amount of the organic additive that described slurries add is 0.1～0.3% of salt slurry quality.
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Cited By (3)
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| CN105664695A (en) * | 2016-02-02 | 2016-06-15 | 新疆青松环保科技股份有限公司 | Wet desulfurization agent and preparation method thereof |
| CN106495187A (en) * | 2016-10-25 | 2017-03-15 | 南京工业大学 | Zero-discharge production process for refining liquid salt by double-membrane method |
| CN108211759A (en) * | 2016-12-22 | 2018-06-29 | 中国石油天然气股份有限公司 | Treatment method and application of salt mud waste generated in chlor-alkali industry |
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| CN101632896A (en) * | 2009-08-03 | 2010-01-27 | 山东山大能源环境有限公司 | Wet flue gas desulfurization process using waste salt slurry |
| CN102961957A (en) * | 2012-12-20 | 2013-03-13 | 新疆鑫恒发环保科技有限公司 | Synergistic limestone desulfuration absorbent |
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| CN105664695A (en) * | 2016-02-02 | 2016-06-15 | 新疆青松环保科技股份有限公司 | Wet desulfurization agent and preparation method thereof |
| CN106495187A (en) * | 2016-10-25 | 2017-03-15 | 南京工业大学 | Zero-discharge production process for refining liquid salt by double-membrane method |
| CN106495187B (en) * | 2016-10-25 | 2018-06-26 | 南京工业大学 | Zero-discharge production process for refining liquid salt by double-membrane method |
| CN108211759A (en) * | 2016-12-22 | 2018-06-29 | 中国石油天然气股份有限公司 | Treatment method and application of salt mud waste generated in chlor-alkali industry |
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Inventor after: Chen Liuping Inventor after: Hao Jianbo Inventor after: Yuan Bin Inventor after: Xie Xingsheng Inventor before: Han Feng Inventor before: Chen Liuping Inventor before: Hao Jianbo Inventor before: Yuan Bin Inventor before: Xie Xingsheng |