CN103848445A - Technique for preparing magnesium sulfate heptahydrate and concentrated sulfuric acid from liquid sulfur dioxide combined with sulfur dioxide - Google Patents
Technique for preparing magnesium sulfate heptahydrate and concentrated sulfuric acid from liquid sulfur dioxide combined with sulfur dioxide Download PDFInfo
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Abstract
The invention discloses a technique for preparing magnesium sulfate heptahydrate and a concentrated sulfuric acid from liquid sulfur dioxide combined with sulfur dioxide. The technique comprises the following procedures: slurry preparation, acidification reaction, gas-phase mist and dust removal, gas-phase drying, pressurized liquefaction, sulfuric acid preparation, liquid-phase neutralization, serous fluid edulcoration, crystallization, solid-liquid separation, drying, packaging and the like. The technique is characterized by comprising the following steps: injecting water into a pulp preparing tank, adding magnesium sulfate to prepare into slurry and pumping into the reaction kettle; adding a concentrated sulfuric acid to react and generate magnesium sulfate and a sulphurous acid, resolving the sulphurous acid into sulfur dioxide and water, wherein the gas-phase sulfur dioxide overflows from the reaction system in the reaction process, drying a part of sulfur dioxide by the concentrated sulfuric acid and compressing and liquefying by a compressor to obtain a liquid sulfur dioxide product; drying a part of sulfur dioxide and then entering into two-rotation and two-absorption sulphuric acid device to prepare the concentrated sulfuric acid. The technique has the beneficial effects that comprehensive utilization of a magnesium desulphurization by-product is achieved, and the technique is applicable to preparation of the magnesium sulfate heptahydrate and the concentrated sulfuric acid from the liquid sulfur dioxide combined with the sulfur dioxide from the magnesium desulphurization by-product in an acidification manner.
Description
Technical field
The invention belongs to flue gas desulfurization technique field, particularly a kind ofly prepare the technology that magnesium sulfate heptahydrate and liquid sulfur dioxide associating sulfurous gas is prepared the vitriol oil.
Background technology
The desulfurization of magnesium method is current conventional fume desulphurization method.In traditional technology, the processing of magnesium method desulfurizing byproduct has two kinds of methods: one is directly to aeration in desulfurization side product magnesium sulfite waste liquid, produces magnesium sulfate finished product.Its shortcoming is that magnesium sulfite aeration effect is bad, and magnesium sulfate content is low, and magnesium sulfate purity is low, and production cost is higher.Another is to add industrial waste sulfuric acid in desulfurization side product magnesium sulfite, produces magnesium sulfate finished product and liquid sulfur dioxide finished product.Its shortcoming is that process is more complicated, and raw material adopts industrial waste sulfuric acid, higher to equipment requirements.Existing sulfurous gas preparation method adopts roasting sulphur or sulphur iron ore, generates sulfurous gas, in roasting and process of lapping, produces dust, and environment is produced and polluted.
Patent 200510086387.8, a kind of magnesium oxide flue gas desulfurization and product thick slurry process oxid-reclamatiom technique, adopt and in circulating absorption solution sweetening process, separate and draw underflow liquid, then blast air, and use steam heating temperature adjustment, the underflow of once desulfurization product magnesium sulfite is oxidized to magnesium sulfate.Its technique is terse reliable, but still belongs to aeration method type.Sulfur dioxide gas in waste liquid is failed to reclaim.
Patent 200810180890.3, one is prepared magnesium sulfate heptahydrate and liquid sulfur dioxide technique, in desulfurization side product magnesium sulfite, adds industrial waste sulfuric acid, produces magnesium sulfate finished product and liquid sulfur dioxide finished product.Comprise the operations such as oxidizing reaction, acid-base neutralisation, slurries removal of impurities, solid-liquid separation, crystallizing and drying, finished product packing, technological process relative complex is higher to equipment requirements.
Patent 201210141185.9, a kind of technique that fully utilizes magnesium method desulfurizing byproduct and produce magnesium sulfate heptahydrate and liquid sulfur dioxide, produces magnesium sulfate finished product and liquid sulfur dioxide finished product.Comprise slurry preparation, add acid-respons, the operation such as gas phase is dry, pressurized liquefied, slurries removal of impurities, crystallization, solid-liquid separation, dry, filter residue sedimentation, in technological process, gas phase is dry thorough not, the more difficult realization of slurries removal of impurities and solid-liquid separation, product liquid sulfur dioxide market is limited.
Summary of the invention
The present invention is the improvement to patent 201210141185.9, the object of this invention is to provide a kind of technology that magnesium sulfate heptahydrate and liquid sulfur dioxide associating sulfurous gas is prepared the vitriol oil of preparing, by add the vitriol oil in magnesium sulfite slurry, generate magnesium sulfate and sulfurous acid through replacement(metathesis)reaction, sulfitolysis generates water and sulfurous gas, in reaction process, gas phase sulfurous gas overflows from reaction system, after electrostatic precipitator demist, part sulfurous gas is dry through the two-stage vitriol oil, compress and liquefy and obtain liquid sulfur dioxide finished product through compressor, another part sulfurous gas is through adding wherein a certain amount of air, sulfuric acid apparatus through double conversion and double absorption is prepared the vitriol oil, raw material as this technique uses, liquid phase is through slurries removal of impurities, crystallization, solid-liquid separation, dry, make magnesium sulfate heptahydrate finished product, realize the comprehensive utilization of magnesium desulfurizing byproduct containing magnesium sulfite.
For achieving the above object, the present invention takes following technical scheme: a kind ofly prepare the technology that magnesium sulfate heptahydrate and liquid sulfur dioxide associating sulfurous gas is prepared the vitriol oil, comprise slurry preparation, add acid-respons, gas phase demist dedusting, gas phase are dry, pressurized liquefied, sulfuric acid preparation, liquid phase neutralization, slurries removal of impurities, crystallization, solid-liquid separation, dry, packaging process, its concrete operation is:
(1) slurry preparation: inject a certain amount of water in pond with slurry, stir, drop into a certain amount of magnesium sulfite, in pond with slurry, the mass ratio of water injection rate and magnesium sulfite input amount is 1: 2.5～1: 3.5, and ratio will strictly be controlled, and slurry will be prepared evenly.
(2) add acid-respons: the magnesium sulfite slurry pump preparing is squeezed in reactor, in reactor, add the vitriol oil, in reactor, the replacement(metathesis)reaction of magnesium sulfite and vitriol oil generation strong acid weak acid processed, generate magnesium sulfate and sulfurous acid, there is decomposition reaction in sulfurous acid self, generates water and sulfurous gas; Reaction process is very violent, can produce a large amount of sulfur dioxide gas, so there will be a large amount of bubbles in reactor, even can produce certain malleation, for guaranteeing that the vitriol oil can be added in reactor as early as possible, promote carrying out smoothly of reaction, need in acid adding tank, be pressed into the malleation of 0.1MPa with air compressor, guarantee to add the speed of the vitriol oil in reactor, enhance productivity.According to the response situation in reactor, control to the speed that adds the vitriol oil in reactor, avoid accidents, temperature of reaction is controlled at 75 ℃ ± 5 ℃, the amount that adds the vitriol oil in reactor is in pond with slurry, to add 41% of magnesium sulfite quality, after all joining in reactor, stirs 20 minutes the vitriol oil in acid adding tank reaction terminating.
(3) gas phase demist dedusting: the wet sulfur dioxide gas producing in acid adding reaction process is sent into gas holder, after gas holder buffering, enter electrostatic precipitator, remove acid mist and the assorted dirt in gas phase through electrostatic precipitator, avoid acid mist and assorted dirt in gas phase to impact the normal operation of the sulfurous gas compressor in subsequent production process and sulfuric acid apparatus.
(4) gas phase is dry: the gas phase sulfurous gas part after electrostatic precipitator demist dedusting is delivered to liquid SO
2the drying tower of device, dry through two-stage, with the moisture content in 93% sulfuric acid spray-absorption furnace gas, make the moisture content in furnace gas be down to 0.05g/m
3following liquor charging state SO
2compression set; Another part, after adding air, makes SO
2concentration reaches 8.5%, now O
2concentration is 19.22%, enters drying tower, with the moisture content in 93% sulfuric acid spray-absorption furnace gas, makes the moisture content in furnace gas be down to 0.1g/m
3below, enter sulfuric acid apparatus conversion section through tower top wire cloth except after Droplets Droplets.
(5) pressurized liquefied: through electrostatic precipitator demist dedusting, two-stage sulfuric acid spray drying, moisture content is down to 0.05g/m
3following dry sulfur dioxide gas, through sulfur dioxide gas gas compressor, is compressed to 0.7MPa by compressor from normal pressure, and after condenser condenses, liquefaction is liquid sulfur dioxide finished product.
(6) sulfuric acid preparation: through electrostatic precipitator demist dedusting, add air, sulfuric acid spray drying, moisture content is down to 0.1g/m
3following dry sulfur dioxide gas, enters sulfuric acid apparatus conversion section through tower top wire cloth except after Droplets Droplets, from convertor reforming gas out in a suction tower with 98% sulfuric acid absorption SO wherein
3, after tower top wire cloth Chu Droplets Droplets, entering again conversion section and transform for the second time, convertor twice transformation gas out enters two suction towers, and tower is interior with 98% sulfuric acid absorption SO wherein
3, after tower top wire cloth Chu Droplets Droplets, through tail gas absorber, discharged by the aiutage of total absolute altitude 45m.
(7) liquid phase neutralization: after reaction finishes, in reactor, solution acidic is stronger, and pH value is about 1, a certain amount of 20% magnesium oxide slurry need to be joined in reactor, the pH value of reaction system is adjusted to 5 to 7, to avoid the producing problem such as quality product and equipment corrosion in subsequent technique.
(8) slurries removal of impurities: after slurry pH value is adjusted to 5～7 in reactor, start filter operation, the neutral hot filtrate of 75 ℃ ± 5 ℃ obtaining through plate-and-frame filter press press filtration is discharged in crystallizer, after press filtration finishes, with pressurized air blowback filter pressing pump, press filtration pipeline and plate-and-frame filter press, can obtain more filtrate, dry up filter cake simultaneously, after blowback finishes, carry out discharging and the work of cleaning sheet frame, water rinses reactor, prevents feed liquid obstruction discharge gate.
(9) crystallization: saturated Adlerika is filtered in crystallizer is stirred, is lowered the temperature in crystallizer, realizes the crystallization of magnesium sulfate, and crystallization terminal temperature is controlled at below 40 ℃.
(10) solid-liquid separation: saturated Adlerika after sufficient crystallising, through centrifuge dewatering, obtains magnesium sulfate heptahydrate crystal product in crystallizer, the needs that require according to client to water ratio can directly be packed sale, also can continue dry rear sale.
(11) dry: the magnesium sulfate crystallization after dehydration is transported in vibrated fluidized bed, is to be dried under 120 ℃ of conditions in temperature, finally obtains dry magnesium sulfate heptahydrate finished product.
(12) packing: magnesium sulfate heptahydrate after drying enters wrapping machine packing by material-conveying belt, according to selling needs, can be packaged into finished product according to 10 kilograms, 20 kilograms, 25 kilograms equal-specifications, and transportation enters warehouse.
A kind of technology that magnesium sulfate heptahydrate and liquid sulfur dioxide associating sulfurous gas is prepared the vitriol oil of preparing as above, its reactor is a kind of enamel reaction still of jacketed, top is provided with vitriol oil import, slurry import, the outlet of gas phase sulfurous gas, gauge port, thermometer mouth, upper flange, bottom is provided with lower flange, discharge port, middle part is provided with chuck, chuck venting port, catalyst import, catalyst outlet, and centre is provided with agitator.
A kind of technology that magnesium sulfate heptahydrate and liquid sulfur dioxide associating sulfurous gas is prepared the vitriol oil of preparing as above, its plate-and-frame filter press is made up of filter frame, filter plate, frame, mechanical clamping device, opening, discharge hole, filtrate receiver.
Positively effect of the present invention is: realized the comprehensive utilization of magnesium method desulfurizing byproduct.The shortcomings such as the rear magnesium sulfate concentration of magnesium sulfite aeration oxidation is low, water content is large are avoided.System does not arrange aeration oxidation unit, saves a large amount of energy consumptions.Reduce the processes such as acid-base neutralisation, realized the simplification of technique.When producing magnesium sulfate finished product, produced the liquid sulfur dioxide finished product of part high added value, part sulfurous gas can be used for producing the vitriol oil, can be used as the raw material of this Technology, has solved the question of market of liquid sulfur dioxide.Be applicable to magnesium desulfurizing byproduct containing magnesium sulfite and prepare the technology that magnesium sulfate heptahydrate and liquid sulfur dioxide associating sulfurous gas is prepared the vitriol oil.
Accompanying drawing explanation
Fig. 1 is that a kind of magnesium method desulfurizing byproduct that utilizes is produced the process flow sheet that magnesium sulfate heptahydrate and liquid sulfur dioxide associating sulfurous gas is prepared the vitriol oil
Fig. 2 is the structural representation of the reactor while adding acid-respons
The structural representation of plate-and-frame filter press when Fig. 3 is slurries removal of impurities
In Fig. 2,1-Despumation device, 2-tensimeter, 3-thermometer, 4-upper cover, 5-upper flange, 6-catalyst venting port, 7-frame type stirring device, 8-direct tube section, 9-chuck, 10-lower flange, 11-lower cover, 101-blow-down pipe, 102-adds acid tube, 103-wash tub pipe, 104-filling tube, 105-catalyst inlet pipe, 106-pressurized air (water) pipe, 107-escape pipe, 108-catalyst outlet pipe, 109-discharge nozzle, 110-scum pipe.
In Fig. 3,21-filter frame, 22-filter plate, 23-frame, 24-mechanical clamping device, 25-opening, 26-discharge hole, 27-filtrate receiver, 201-compressed air pipe, 202-feed-pipe, 203-wash tub pipe, 204-discharge nozzle, 205-discharging tube.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is described in detail.
As shown in Figure 1, the present invention is a kind of technology that magnesium sulfate heptahydrate and liquid sulfur dioxide associating sulfurous gas is prepared the vitriol oil of preparing, comprise slurry preparation, add acid-respons, gas phase demist dedusting, gas phase are dry, pressurized liquefied, sulfuric acid preparation, liquid phase neutralization, slurries removal of impurities, crystallization, solid-liquid separation, dry, packaging process, its concrete operation is:
(1) slurry preparation: inject a certain amount of water in pond with slurry, stir, drop into a certain amount of magnesium sulfite, in pond with slurry, the mass ratio of water injection rate and magnesium sulfite input amount is 1: 2.5～1: 3.5, and ratio will strictly be controlled, and slurry will be prepared evenly.
(2) add acid-respons: the magnesium sulfite slurry pump preparing is squeezed in reactor, in reactor, add the vitriol oil, in reactor, the replacement(metathesis)reaction of magnesium sulfite and vitriol oil generation strong acid weak acid processed, generate magnesium sulfate and sulfurous acid, there is decomposition reaction in sulfurous acid self, generates water and sulfurous gas; Reaction process is very violent, can produce a large amount of sulfur dioxide gas, so there will be a large amount of bubbles in reactor, even can produce certain malleation, for guaranteeing that the vitriol oil can be added in reactor as early as possible, promote carrying out smoothly of reaction, need in acid adding tank, be pressed into the malleation of 0.1MPa with air compressor, guarantee to add the speed of the vitriol oil in reactor, enhance productivity.According to the response situation in reactor, control to the speed that adds the vitriol oil in reactor, avoid accidents, temperature of reaction is controlled at 75 ℃ ± 5 ℃, the amount that adds the vitriol oil in reactor is in pond with slurry, to add 41% of magnesium sulfite quality, after all joining in reactor, stirs 20 minutes the vitriol oil in acid adding tank reaction terminating.
(3) gas phase demist dedusting: the wet sulfur dioxide gas producing in acid adding reaction process is sent into gas holder, after gas holder buffering, enter electrostatic precipitator, remove acid mist and the assorted dirt in gas phase through electrostatic precipitator, avoid acid mist and assorted dirt in gas phase to impact the normal operation of the sulfurous gas compressor in subsequent production process and sulfuric acid apparatus.
(4) gas phase is dry: the gas phase sulfurous gas part after electrostatic precipitator demist dedusting is delivered to liquid SO
2the drying tower of device, dry through two-stage, with the moisture content in 93% sulfuric acid spray-absorption furnace gas, make the moisture content in furnace gas be down to 0.05g/m
3following liquor charging state SO
2compression set; Another part, after adding air, makes SO
2concentration reaches 8.5%, now O
2concentration is 19.22%, enters drying tower, with the moisture content in 93% sulfuric acid spray-absorption furnace gas, makes the moisture content in furnace gas be down to 0.1g/m
3below, enter sulfuric acid apparatus conversion section through tower top wire cloth except after Droplets Droplets.
(5) pressurized liquefied: through electrostatic precipitator demist dedusting, two-stage sulfuric acid spray drying, moisture content is down to 0.05g/m
3following dry sulfur dioxide gas, through sulfur dioxide gas gas compressor, is compressed to 0.7MPa by compressor from normal pressure, and after condenser condenses, liquefaction is liquid sulfur dioxide finished product.
(6) sulfuric acid preparation: through electrostatic precipitator demist dedusting, add air, sulfuric acid spray drying, moisture content is down to 0.1g/m
3following dry sulfur dioxide gas, enters sulfuric acid apparatus conversion section through tower top wire cloth except after Droplets Droplets, from convertor reforming gas out in a suction tower with 98% sulfuric acid absorption SO wherein
3, after tower top wire cloth Chu Droplets Droplets, entering again conversion section and transform for the second time, convertor twice transformation gas out enters two suction towers, and tower is interior with 98% sulfuric acid absorption SO wherein
3, after tower top wire cloth Chu Droplets Droplets, through tail gas absorber, discharged by the aiutage of total absolute altitude 45m.
(7) liquid phase neutralization: after reaction finishes, in reactor, solution acidic is stronger, and pH value is about 1, a certain amount of 20% magnesium oxide slurry need to be joined in reactor, the pH value of reaction system is adjusted to 5 to 7, to avoid the producing problem such as quality product and equipment corrosion in subsequent technique.
(8) slurries removal of impurities: after slurry pH value is adjusted to 5～7 in reactor, start filter operation, the neutral hot filtrate of 75 ℃ ± 5 ℃ obtaining through plate-and-frame filter press press filtration is discharged in crystallizer, after press filtration finishes, with pressurized air blowback filter pressing pump, press filtration pipeline and plate-and-frame filter press, can obtain more filtrate, dry up filter cake simultaneously, after blowback finishes, carry out discharging and the work of cleaning sheet frame, water rinses reactor, prevents feed liquid obstruction discharge gate.
(9) crystallization: saturated Adlerika is filtered in crystallizer is stirred, is lowered the temperature in crystallizer, realizes the crystallization of magnesium sulfate, and crystallization terminal temperature is controlled at below 40 ℃.
(10) solid-liquid separation: saturated Adlerika after sufficient crystallising, through centrifuge dewatering, obtains magnesium sulfate heptahydrate crystal product in crystallizer, the needs that require according to client to water ratio can directly be packed sale, also can continue dry rear sale.
(11) dry: the magnesium sulfate crystallization after dehydration is transported in vibrated fluidized bed, is to be dried under 120 ℃ of conditions in temperature, finally obtains dry magnesium sulfate heptahydrate finished product.
(12) packing: magnesium sulfate heptahydrate after drying enters wrapping machine packing by material-conveying belt, according to selling needs, can be packaged into finished product according to 10 kilograms, 20 kilograms, 25 kilograms equal-specifications, and transportation enters warehouse.
As shown in Figure 2, a kind ofly prepare the technology that magnesium sulfate heptahydrate and liquid sulfur dioxide associating sulfurous gas is prepared the vitriol oil, reactor while adding acid-respons is a kind of enamel reaction still of jacketed, can avoid reactor to be corroded, can bear pressure more than 0.3MPa, comprise reactor body, chuck, feed-pipe, discharge nozzle, scum pipe, escape pipe, add acid tube, wash tub pipe, blow-down pipe, pressurized air (water) pipe, whipping appts, reactor body is by the upper cover 4 at direct tube section 8 and upper and lower two ends, lower cover 11 forms, described direct tube section is connected with upper flange 5 with upper cover, direct tube section is connected with lower flange 10 with lower cover, the top of described upper cover is provided with feed-pipe 104, escape pipe 107, add acid tube 102, blow-down pipe 101, tensimeter 2 and thermometer 3, described lower cover is provided with discharge nozzle 109, described feed-pipe is provided with wash tub pipe 103, described discharge nozzle is provided with pressurized air (water) pipe 106 and scum pipe 110, described escape pipe is provided with Despumation device 1, the direct tube section outer wall of described reactor is provided with chuck 9, the bottom of described chuck is provided with catalyst inlet pipe 105, the top of described chuck is provided with catalyst outlet pipe 108, catalyst venting port 6, reactor inwall is enamel structure, be provided with frame type stirring device 7 in reactor inside.
As shown in Figure 3, a kind ofly prepare the technology that magnesium sulfate heptahydrate and liquid sulfur dioxide associating sulfurous gas is prepared the vitriol oil, plate-and-frame filter press when slurries removal of impurities, is made up of staggered polylith filter plate, filter frame and the mechanical clamping device being assembled in frame.On the surface of described filter plate 22 and filter frame 21 with ups and downs filtrate channel, described filter plate 22, filter frame 21 both sides have identical opening 25, the mutual UNICOM of opening on described all filter plates, the transfer passage of formation slurries, pressurized air and wash-down water; Described filter frame 21 is connected with feed-pipe 202 by described opening 25, and described feed-pipe is provided with compressed air pipe 201 and wash tub pipe 203, forms charging, the rinse-system of plate-and-frame filter press.Below each filter plate, be provided with discharge hole 26 and discharge nozzle 204, described discharge nozzle 204 is communicated on described discharge hole 26, and the bottom of described discharge nozzle 204 is provided with filtrate receiver 7, and as the interim receiving trap of filtrate, the bottom of described filtrate receiver 27 is provided with discharging tube 205.Plate-and-frame filter press is fixed in frame 23, and power set is the mechanical clamping device 24 of described frame 23 rear sides.
Claims (3)
1. prepare the technology that magnesium sulfate heptahydrate and liquid sulfur dioxide associating sulfurous gas is prepared the vitriol oil for one kind, comprise slurry preparation, add acid-respons, gas phase demist dedusting, gas phase are dry, pressurized liquefied, sulfuric acid preparation, liquid phase neutralization, slurries removal of impurities, crystallization, solid-liquid separation, dry, packaging process, it is characterized in that:
(1) slurry preparation: inject a certain amount of water in pond with slurry, stir, drop into a certain amount of magnesium sulfite, in pond with slurry, the mass ratio of water injection rate and magnesium sulfite input amount is 1: 2.5～1: 3.5, and ratio will strictly be controlled, and slurry will be prepared evenly;
(2) add acid-respons: the magnesium sulfite slurry pump preparing is squeezed in reactor, in reactor, add the vitriol oil, in reactor, the replacement(metathesis)reaction of magnesium sulfite and vitriol oil generation strong acid weak acid processed, generate magnesium sulfate and sulfurous acid, there is decomposition reaction in sulfurous acid self, generates water and sulfurous gas; Reaction process is very violent, can produce a large amount of sulfur dioxide gas, so there will be a large amount of bubbles in reactor, even can produce certain malleation, for guaranteeing that the vitriol oil can be added in reactor as early as possible, promote carrying out smoothly of reaction, need in acid adding tank, be pressed into the malleation of 0.1MPa with air compressor, guarantee to add the speed of the vitriol oil in reactor, enhance productivity.According to the response situation in reactor, control to the speed that adds the vitriol oil in reactor, avoid accidents, temperature of reaction is controlled at 75 ℃ ± 5 ℃, the amount that adds the vitriol oil in reactor is in pond with slurry, to add 41% of magnesium sulfite quality, after all joining in reactor, stirs 20 minutes the vitriol oil in acid adding tank reaction terminating;
(3) gas phase demist dedusting: the wet sulfur dioxide gas producing in acid adding reaction process is sent into gas holder, after gas holder buffering, enter electrostatic precipitator, remove acid mist and the assorted dirt in gas phase through electrostatic precipitator, avoid acid mist and assorted dirt in gas phase to impact the normal operation of the sulfurous gas compressor in subsequent production process and sulfuric acid apparatus;
(4) gas phase is dry: the gas phase sulfurous gas part after electrostatic precipitator demist dedusting is delivered to liquid SO
2the drying tower of device, dry through two-stage, with the moisture content in 93% sulfuric acid spray-absorption furnace gas, make the moisture content in furnace gas be down to 0.05g/m
3following liquor charging state SO
2compression set; Another part, after adding air, makes SO
2concentration reaches 8.5%, now O
2concentration is 19.22%, enters drying tower, with the moisture content in 93% sulfuric acid spray-absorption furnace gas, makes the moisture content in furnace gas be down to 0.1g/m
3below, enter sulfuric acid apparatus conversion section through tower top wire cloth except after Droplets;
(5) pressurized liquefied: through electrostatic precipitator demist dedusting, two-stage sulfuric acid spray drying, moisture content is down to 0.05g/m
3following dry sulfur dioxide gas, through sulfur dioxide gas gas compressor, is compressed to 0.7MPa by compressor from normal pressure, and after condenser condenses, liquefaction is liquid sulfur dioxide finished product;
(6) sulfuric acid preparation: through electrostatic precipitator demist dedusting, add air, sulfuric acid spray drying, moisture content is down to 0.1g/m
3following dry sulfur dioxide gas, enters sulfuric acid apparatus conversion section through tower top wire cloth except after Droplets, from convertor reforming gas out in a suction tower with 98% sulfuric acid absorption SO wherein
3, after tower top wire cloth Chu Droplets, entering again conversion section and transform for the second time, convertor twice transformation gas out enters two suction towers, and tower is interior with 98% sulfuric acid absorption SO wherein
3, after tower top wire cloth Chu Droplets, through tail gas absorber, discharged by the aiutage of total absolute altitude 45m;
(7) liquid phase neutralization: after reaction finishes, in reactor, solution acidic is stronger, and pH value is about 1, a certain amount of 20% magnesium oxide slurry need to be joined in reactor, the pH value of reaction system is adjusted to 5 to 7, to avoid the producing problem such as quality product and equipment corrosion in subsequent technique;
(8) slurries removal of impurities: after slurry pH value is adjusted to 5～7 in reactor, start filter operation, the neutral hot filtrate of 75 ℃ ± 5 ℃ obtaining through plate-and-frame filter press press filtration is discharged in crystallizer, after press filtration finishes, with pressurized air blowback filter pressing pump, press filtration pipeline and plate-and-frame filter press, can obtain more filtrate, dry up filter cake simultaneously, after blowback finishes, carry out discharging and the work of cleaning sheet frame, water rinses reactor, prevents feed liquid obstruction discharge gate;
(9) crystallization: saturated Adlerika is filtered in crystallizer is stirred, is lowered the temperature in crystallizer, realizes the crystallization of magnesium sulfate, and crystallization terminal temperature is controlled at below 40 ℃;
(10) solid-liquid separation: saturated Adlerika after sufficient crystallising, through centrifuge dewatering, obtains magnesium sulfate heptahydrate crystal product in crystallizer, the needs that require according to client to water ratio can directly be packed sale, also can continue dry rear sale;
(11) dry: the magnesium sulfate crystallization after dehydration is transported in vibrated fluidized bed, is to be dried under 120 ℃ of conditions in temperature, finally obtains dry magnesium sulfate heptahydrate finished product;
(12) packing: magnesium sulfate heptahydrate after drying enters wrapping machine packing by material-conveying belt, according to selling needs, can be packaged into finished product according to 10 kilograms, 20 kilograms, 25 kilograms equal-specifications, and transportation enters warehouse.
2. a kind of technology that fully utilizes magnesium method desulfurizing byproduct and produce magnesium sulfate heptahydrate and liquid sulfur dioxide as claimed in claim 1, is characterized in that: reactor is a kind of enamel reaction still of jacketed, and centre is provided with agitator.
3. a kind of technology that magnesium sulfate heptahydrate and liquid sulfur dioxide associating sulfurous gas is prepared the vitriol oil of preparing as claimed in claim 1, is characterized in that: plate-and-frame filter press is made up of staggered polylith filter plate, filter frame and the mechanical clamping device being assembled in frame.
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| CN110639337A (en) * | 2019-11-01 | 2020-01-03 | 武汉青江化工黄冈有限公司 | SO based on sulphuric acid apparatus for producing2Wet gas extraction process |
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| CN101423234A (en) * | 2008-11-27 | 2009-05-06 | 六合天融（北京）环保科技有限公司 | Process for preparing heptahydrate magnesium sulfate and liquid sulphur dioxide |
| CN102001633A (en) * | 2009-09-02 | 2011-04-06 | 南化集团研究院 | Method for preparing sulfuric acid by using mixture containing magnesium sulfite as raw material |
| CN102101004A (en) * | 2011-01-26 | 2011-06-22 | 中节能六合天融环保科技有限公司 | Method for recovering magnesium oxide and byproduct sulfur dioxide by using indirect heating rotary roasting furnace |
| CN103387247A (en) * | 2012-05-09 | 2013-11-13 | 中节能六合天融环保科技有限公司 | Process for preparing magnesium sulfate heptahydrate and liquid sulfur dioxide by comprehensively utilizing magnesium desulfurization byproducts |
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Application publication date: 20140611 |