CN214087744U - Device for concentrating and recovering magnesium sulfate heptahydrate from wet magnesium oxide desulfurization waste liquid - Google Patents
Device for concentrating and recovering magnesium sulfate heptahydrate from wet magnesium oxide desulfurization waste liquid Download PDFInfo
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- CN214087744U CN214087744U CN202022687948.2U CN202022687948U CN214087744U CN 214087744 U CN214087744 U CN 214087744U CN 202022687948 U CN202022687948 U CN 202022687948U CN 214087744 U CN214087744 U CN 214087744U
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- 239000007788 liquid Substances 0.000 title claims abstract description 166
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 81
- 230000023556 desulfurization Effects 0.000 title claims abstract description 77
- 239000002699 waste material Substances 0.000 title claims abstract description 29
- 239000000395 magnesium oxide Substances 0.000 title claims abstract description 17
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 title claims abstract description 17
- WRUGWIBCXHJTDG-UHFFFAOYSA-L magnesium sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Mg+2].[O-]S([O-])(=O)=O WRUGWIBCXHJTDG-UHFFFAOYSA-L 0.000 title claims abstract description 15
- 229940061634 magnesium sulfate heptahydrate Drugs 0.000 title claims abstract description 15
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 title claims abstract description 14
- 238000003860 storage Methods 0.000 claims abstract description 40
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 24
- 238000000034 method Methods 0.000 claims abstract description 18
- 230000000694 effects Effects 0.000 claims abstract description 17
- 239000012452 mother liquor Substances 0.000 claims abstract description 14
- 239000012141 concentrate Substances 0.000 claims abstract description 8
- 238000011084 recovery Methods 0.000 claims abstract description 5
- 239000000463 material Substances 0.000 claims description 57
- 239000012535 impurity Substances 0.000 claims description 43
- 230000003009 desulfurizing effect Effects 0.000 claims description 14
- 238000003756 stirring Methods 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 5
- 238000012856 packing Methods 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 abstract description 10
- 238000002425 crystallisation Methods 0.000 abstract description 9
- 230000008025 crystallization Effects 0.000 abstract description 9
- 238000001816 cooling Methods 0.000 abstract description 8
- 230000008020 evaporation Effects 0.000 abstract description 7
- 230000008569 process Effects 0.000 abstract description 7
- 239000012530 fluid Substances 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 description 7
- 239000013078 crystal Substances 0.000 description 7
- 238000004806 packaging method and process Methods 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 238000003825 pressing Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000000926 separation method Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006298 dechlorination reaction Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000006911 nucleation Effects 0.000 description 1
- 238000010899 nucleation Methods 0.000 description 1
- 238000011085 pressure filtration Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The utility model provides a device of wet-type magnesium oxide method desulfurization waste liquid concentration recovery magnesium sulfate heptahydrate, includes edulcoration agent fluid reservoir, desulfurization liquid storage tank, edulcoration reactor, the middle groove of desulfurization liquid, plate and frame filter press, desulfurization clear solution storage tank, I effect evaporator, II effect evaporator, one-level hydrocyclone, flash tank, concentrate fluid reservoir, crystallizer, centrifuge, packagine machine and mother liquor pit. The utility model utilizes the process of evaporation concentration-cooling crystallization to treat the desulfurization waste liquid, realizes zero discharge of the desulfurization waste liquid, reduces the environmental burden, produces magnesium sulfate heptahydrate product simultaneously, changes waste into valuable, and realizes the circular economy treatment of the desulfurization waste liquid; the method has simple process flow and reliable operation.
Description
Technical Field
The utility model belongs to the technical field of smelting, chemical industry, concretely relates to device of wet-type magnesium oxide method desulfurization waste liquid concentration recovery magnesium sulfate heptahydrate.
Background
In recent years, with the development of flue gas desulfurization in China, the wet magnesium oxide flue gas desulfurization technology is widely applied due to the characteristics of high desulfurization efficiency (up to more than 90%), capability of recovering sulfur, capability of avoiding generation of solid waste and the like, but the treatment of desulfurization waste liquid generated in the desulfurization process becomes a difficult problem which needs to be solved urgently. At present, there are three main methods for treating desulfurization waste liquid, i.e., a regeneration method, a disposal method, and a recovery method. The key of the regeneration magnesium desulfurization technology is that pre-dedusting and pre-dechlorination are carried out on flue gas, about 8% of MgO is lost in the process to cause secondary pollution, the temperature must be strictly controlled in the calcining process, the phenomenon of MgO sintering can occur when the temperature is too high, and the part of sintered or hard-burned MgO can not be used as a desulfurizer any more. The abandoning method is to directly discharge the solution containing magnesium sulfate, thereby wasting resources and influencing the ecological environment. The recovery method is to recover magnesium sulfate heptahydrate crystals after the desulfurization waste liquid is oxidized, impurity removed, filtered, evaporated, concentrated, cooled, crystallized and centrifugally separated. Magnesium sulfate heptahydrate can be used as a fertilizer in agriculture, is an important industrial raw material, can be recycled as a magnesium desulphurization raw material, and has high economic value.
SUMMERY OF THE UTILITY MODEL
The utility model provides a device for concentrating and recovering magnesium sulfate heptahydrate from wet-type magnesium oxide desulfurization waste liquid, which comprises an impurity removal agent liquid tank, a desulfurization liquid storage tank, an impurity removal reactor, a desulfurization liquid intermediate tank, a plate-and-frame filter press, a desulfurization clear liquid storage tank, a first-effect evaporator, a second-effect evaporator, a first-stage hydrocyclone, a flash tank, a concentrated liquid tank, a crystallizing tank, a centrifugal separator, a packaging machine and a mother liquid pit; the device comprises an impurity removing agent liquid tank, a desulfurization liquid storage tank, a plate-and-frame filter press, a desulfurization clear liquid storage tank, a first-effect evaporator, a second-effect evaporator, a steam header pipe, a second-effect evaporator, a vacuum pump, a first-effect liquid separator, a second-effect liquid separator, a desulfurization liquid storage tank, a desulfurization liquid intermediate tank, a first-effect evaporator, a second-effect evaporator and a desulfurization liquid storage tank, wherein the impurity removing agent liquid tank and the desulfurization liquid storage tank are respectively connected through a bottom liquid discharge pipeline, the desulfurization liquid intermediate tank is connected with the plate-and-frame filter press through a filter press pump arranged at the bottom of the desulfurization liquid intermediate tank, the plate-and-frame filter press is connected with the desulfurization clear liquid storage tank through a bottom liquid discharge pipeline, the desulfurization clear liquid storage tank is connected with the first-effect evaporator through a feed pump arranged at the bottom of the desulfurization clear liquid intermediate tank, the first-effect evaporator is connected with the second-effect evaporator through a steam valve, the second-effect evaporator is connected with a first-effect liquid cyclone separator through a gas exhaust pipeline at the top of the bottom of the second-effect evaporator, one-level hydrocyclone passes through the bottom drain line and links to each other with the flash tank, the flash tank links to each other with the concentrate jar through the flash pump that sets up in its bottom, the concentrate jar links to each other with the crystallizer through the concentrate pump that sets up in its bottom, the crystallizer is equipped with crystallizer stirring and crystallizer blow-off valve, and the crystallizer links to each other with centrifuge through its bottom drain line, the centrifuge lower part is provided with the belt, and the belt links to each other with packagine machine, centrifuge bottom mother liquor pipeline links to each other with the mother liquor pit, the mother liquor pit returns to I effect evaporator through the pit pump.
And the desulfurization liquid storage tank and the impurity removal reactor are directly provided with a desulfurization liquid delivery pump.
The automatic feeding device is characterized in that an outlet of the feeding pump is provided with an automatic discharge valve and a liquid level interlock of the first-effect evaporator, an automatic material stringing valve is arranged on a material passing pipeline between the first-effect evaporator and the second-effect evaporator, the automatic material stringing valve is interlocked with the liquid level of the second-effect evaporator, and the top of the first-stage hydrocyclone separator is provided with a backflow valve which is connected with a feeding pipeline of the second-effect evaporator.
And a densimeter arranged on an outlet pipeline of the flash tank is interlocked with a crystallizing tank feeding valve arranged on the crystallizing tank.
The utility model has the advantages that:
1. the utility model discloses utilize double-effect second grade evaporation concentration + first-order adiabatic flash distillation + buffering cooling, triple production technology of stirring crystallization, add the edulcoration agent with the desulfurization waste liquid and detach heavy metal ion, carry the desulfurization waste liquid after the edulcoration to the plate frame pressure filter through the filter press, the clear solution is carried to the clear solution storage tank after the filter press filter, carry to I effect evaporator in through the charge pump, carry to II effect evaporator in through the charge pump after the first-order evaporation concentration, further evaporation concentration in II effect evaporator, after reaching the supersaturated concentration, carry to the flash tank by the charge pump and carry out adiabatic evaporation, carry to concentrated fluid reservoir buffer by the flash pump and cool off, carry to the crystallizer through the concentrated fluid pump again and carry out cooling crystallization, after crystallization nucleation is grown up, discharge to centrifuge by the crystallizer, after centrifuge centrifugal separation, finished product percutaneous area is transported to packagine machine packing pile up neatly, the mother liquor returns to the evaporator for reuse.
2. The method of the utility model mainly uses the desulfurization waste liquid as the raw material to produce the magnesium sulfate heptahydrate product with certain economic value; the utility model discloses a series of automatic interlocking control, the charge pump export of desulfurization clear solution storage tank bottom is equipped with automatic bleeder valve and I effect evaporimeter liquid level interlocking, is provided with automatic cluster material valve on the material pipeline of crossing between I effect evaporimeter and II effect evaporimeters, and automatic cluster material valve and II effect evaporimeter liquid level interlocking are equipped with the backwash valve at one-level hydrocyclone separator top and link to each other with II effect evaporimeter charge-in pipeline. The flash tank is provided with a densimeter which is interlocked with a feed valve of the crystallizing tank. And finally, the aim of balancing the material inlet and outlet is fulfilled through interlocking control.
3. The utility model utilizes the process of evaporation concentration-cooling crystallization to treat the desulfurization waste liquid, realizes zero discharge of the desulfurization waste liquid, reduces the environmental burden, produces magnesium sulfate heptahydrate product simultaneously, changes waste into valuable, and realizes the circular economy treatment of the desulfurization waste liquid; the method has simple process flow and reliable operation.
Drawings
The following describes the embodiments of the present invention in further detail with reference to the accompanying drawings.
Fig. 1 is a schematic flow chart of the present invention.
In the figure: 1-edulcoration agent liquid tank 2-desulfurization liquid storage tank 3-edulcoration reactor 4-desulfurization liquid intermediate tank 5-plate-and-frame filter press 6-desulfurization clear liquid storage tank 7-effect evaporator 8-effect evaporator 9-first-stage hydrocyclone 10-flash tank 11-concentrated liquid tank 12-crystallizing tank 13-centrifugal separator 14-belt 15-packaging machine 16-mother liquid pit 17-desulfurization liquid delivery pump 18-pressure filtration pump 19-feeding pump 20-steam valve 21-effect material passing pump 22-material passing valve 23-effect material passing pump 24-clear liquid reflux valve 25-flash evaporation pump 26-concentrated liquid feeding pump 27-mother liquid pit pump 28-vacuum pump 29-crystallizing tank feeding valve 30-crystallizing tank stirring 31-crystallizing tank discharge valve 32-discharge valve 33-densimeter.
Detailed Description
The device for concentrating and recovering magnesium sulfate heptahydrate from wet magnesium oxide desulfurization waste liquid comprises an impurity removal agent liquid tank 1, a desulfurization liquid storage tank 2, an impurity removal reactor 3, a desulfurization liquid intermediate tank 4, a plate-and-frame filter press 5, a desulfurization clear liquid storage tank 6, an I-effect evaporator 7, an II-effect evaporator 8, a primary hydrocyclone 9, a flash tank 10, a concentrate liquid tank 11, a crystallizing tank 12, a centrifugal separator 13, a packing machine 15 and a mother liquid pit 16; an impurity removing agent solution tank 1 and a desulfurizing solution storage tank 2 are respectively connected with an impurity removing reactor 3 through a bottom liquid discharge pipeline, the impurity removing reactor 3 is connected with a desulfurizing solution intermediate tank 4 through a bottom liquid discharge pipeline, the desulfurizing solution intermediate tank 4 is connected with a plate-and-frame filter press 5 through a filter press pump 18 arranged at the bottom of the desulfurizing solution intermediate tank, the plate-and-frame filter press 5 is connected with a desulfurizing clear solution storage tank 6 through a bottom liquid discharge pipeline, the desulfurizing clear solution storage tank 6 is connected with an I-effect evaporator 7) through a feed pump 19 arranged at the bottom of the desulfurizing solution intermediate tank, the I-effect evaporator 7 is connected with a II-effect evaporator 8 through an I-effect material passing pump 21 arranged at the bottom of the I-effect evaporator, the I-effect evaporator 7 is connected with a steam main pipe through a steam valve 20, secondary steam generated by the I-effect evaporator 7 is connected with the II-effect evaporator 8 through a top steam pipeline, the top of the II-effect evaporator 8 is connected with a vacuum pump 28 through an air exhaust pipeline, the II-effect evaporator 8 is connected with a primary hydrocyclone 9 through an II-effect material passing pump 23 arranged at the bottom of the II-effect evaporator, the primary hydrocyclone 9 is connected with the flash tank 10 through a bottom liquid discharge pipeline, the flash tank 10 is connected with a concentrated liquid tank 11 through a flash pump 25 arranged at the bottom of the flash tank, the concentrated liquid tank 11 is connected with a crystallizing tank 12 through a concentrated liquid pump 26 arranged at the bottom of the crystallizing tank, the crystallizing tank 12 is provided with a crystallizing tank stirrer 30 and a crystallizing tank discharge valve 31, the crystallizing tank 12 is connected with a centrifugal separator 13 through a bottom liquid discharge pipeline, the lower part of the centrifugal separator 13 is provided with a belt 14, the belt 14 is connected with a packing machine 15, a mother liquid pipeline at the bottom of the centrifugal separator 13 is connected with a mother liquid pit 16, and the mother liquid pit 16 returns to the I-effect evaporator 7 through a pit pump 27.
The doctor solution storage tank 2 and the impurity removal reactor 3 are directly provided with a doctor solution delivery pump 17.
An outlet of the feed pump 19 is provided with an automatic discharge valve 32 interlocked with the liquid level of the first-effect evaporator 7, an automatic material mixing valve 22 is arranged on a material passing pipeline between the first-effect evaporator 7 and the second-effect evaporator 8, the automatic material mixing valve 22 is interlocked with the liquid level of the second-effect evaporator 8, and the top of the primary hydrocyclone 9 is provided with a reflux valve 24 connected with the feed pipeline of the second-effect evaporator 8.
A densitometer 33 provided in the outlet line of the flash tank 10 is interlocked with a crystallizer feed valve 29 provided in the crystallizer 12.
The material flow is as follows: the desulfurization waste liquid after magnesium oxide desulfurization is stored in a desulfurization liquid storage tank 2, is conveyed to an impurity removal reactor 3 through a desulfurization liquid conveying pump 17, is subjected to impurity removal reaction with a liquid impurity removal agent reacted in an impurity removal agent liquid tank 1, enters a desulfurization liquid intermediate tank 4 under self pressure after impurity removal, is conveyed to a plate-and-frame filter press 5 through a filter press pump 18 for filter pressing, and enters a desulfurization clear liquid storage tank 6; clear liquid in a desulfurized clear liquid storage tank 6 is conveyed to a first-effect evaporator 7 through a feed pump 19, when the liquid level reaches a certain height, an automatic material stringing valve 22 is opened, a first-effect material passing pump 21 is started to feed materials to a second-effect evaporator 8, and when the material liquid of the second-effect evaporator 8 reaches a certain height, a steam valve 20 is opened to heat the material liquid in the effect body; when crystal particles appear on a viewing mirror of the II-effect evaporator 8, starting the II-effect material passing pump 23 to feed into the primary hydrocyclone 9, simultaneously opening a return valve 24 of the primary hydrocyclone, automatically adjusting the liquid level of the primary hydrocyclone 9 according to liquid level interlocking, discharging the primary hydrocyclone to the flash tank 10 under self-pressure, and automatically evaporating in the flash tank 10; when the density of the materials in the flash tank 10 reaches a certain value, starting a flash pump 25 to feed the concentrated solution storage tank 11, when the liquid level reaches a certain height, opening a crystallizing tank feeding valve 29, starting a concentrated solution pump 26 to feed the materials into the crystallizing tank 12, when the liquid level of the crystallizing tank 12 reaches a certain height, starting the crystallizing tank to stir 30, and cooling and crystallizing the materials by using circulating water; when crystal particles are separated out from the crystallization tank 12, a crystallization tank discharge valve 31 is opened to feed materials into the centrifugal separator 13, the materials are conveyed to a packaging machine 15 through a belt 14 to be packaged after centrifugal separation, and mother liquor enters a mother liquor pit 16 and returns to the I-effect evaporator 7 through a pit pump 27 to be recycled.
Example 1
Manually adding a certain amount of solid impurity removing agent into the impurity removing agent liquid tank 1, opening a water adding valve, dissolving the solid impurity removing agent into a liquid impurity removing agent, storing the desulfurization waste liquid after magnesium oxide desulfurization in a desulfurization liquid storage tank 2, conveying the desulfurization waste liquid to an impurity removing reactor 3 through a desulfurization liquid conveying pump 17, performing impurity removing reaction with the liquid impurity removing agent reacted in the impurity removing agent liquid tank 1, introducing steam for heating in the impurity removing reaction process, controlling the reaction temperature to be 80-90 ℃, conveying the desulfurization liquid after impurity removal into a desulfurization liquid intermediate tank 4 under self pressure, conveying the desulfurization liquid to a plate and frame filter press 5 through a filter press pump 18 for filter pressing, and conveying the clear liquid after filter pressing into a desulfurization clear liquid storage tank 6; clear liquid in a desulfurized clear liquid storage tank 6 is conveyed to a first-effect evaporator 7 through a feed pump 19, when the liquid level reaches a certain height, an automatic material stringing valve 22 is opened, a first-effect material passing pump 21 is started to feed materials to a second-effect evaporator 8, and when the material liquid of the second-effect evaporator 8 reaches a certain height, a steam valve 20 is opened to heat the material liquid in the effect body; controlling the temperature of the material liquid in the first-effect evaporator 7 to be 105-110 ℃, the temperature of the material liquid in the second-effect evaporator 8 to be 80-85 ℃, starting a second-effect material passing pump 23 to feed into the first-stage hydrocyclone 9 when crystal particles appear on a viewing mirror of the second-effect evaporator 8, simultaneously opening a reflux valve 24 of the first-stage hydrocyclone, automatically adjusting the liquid level of the first-stage hydrocyclone 9 according to liquid level interlocking, feeding the first-stage hydrocyclone to a flash tank 10 under the self-pressure, and automatically evaporating in the flash tank 10; when the Baume degree of the materials in the flash tank 10 reaches 1.33g/cm3, starting a flash pump 25 to feed the concentrated solution to a concentrated solution storage tank 11, when the liquid level reaches a certain height, opening a crystallizing tank feeding valve 29, starting a concentrated solution pump 26 to feed the materials into a crystallizing tank 12, when the liquid level of the crystallizing tank 12 reaches a certain height, starting the crystallizing tank to stir 30, and cooling and crystallizing the materials by using circulating water; and cooling and crystallizing for 12-14 h, opening a crystallizing tank discharge valve 31 to feed into a centrifugal separator 13 after crystal particles are separated out from the crystallizing tank 12, conveying the materials to a packaging machine 15 through a belt 14 for packaging after centrifugal separation, and allowing the mother liquor to enter a mother liquor pit 16 and return to the I-effect evaporator 7 through a pit pump 27 for recycling.
Example 2
Manually adding a certain amount of solid impurity removing agent into the impurity removing agent liquid tank 1, opening a water adding valve, dissolving the solid impurity removing agent into a liquid impurity removing agent, storing the desulfurization waste liquid after magnesium oxide desulfurization in a desulfurization liquid storage tank 2, conveying the desulfurization waste liquid to an impurity removing reactor 3 through a desulfurization liquid conveying pump 17, performing impurity removing reaction with the liquid impurity removing agent reacted in the impurity removing agent liquid tank 1, introducing steam for heating in the impurity removing reaction process, controlling the reaction temperature to be 80-90 ℃, conveying the desulfurization liquid after impurity removal into a desulfurization liquid intermediate tank 4 under self pressure, conveying the desulfurization liquid to a plate and frame filter press 5 through a filter press pump 18 for filter pressing, and conveying the clear liquid after filter pressing into a desulfurization clear liquid storage tank 6; clear liquid in a desulfurized clear liquid storage tank 6 is conveyed to a first-effect evaporator 7 through a feed pump 19, when the liquid level reaches a certain height, an automatic material stringing valve 22 is opened, a first-effect material passing pump 21 is started to feed materials to a second-effect evaporator 8, and when the material liquid of the second-effect evaporator 8 reaches a certain height, a steam valve 20 is opened to heat the material liquid in the effect body; controlling the temperature of the material liquid in the first-effect evaporator 7 to be 105-110 ℃, the temperature of the material liquid in the second-effect evaporator 8 to be 80-85 ℃, starting a second-effect material passing pump 23 to feed into the first-stage hydrocyclone 9 when crystal particles appear on a viewing mirror of the second-effect evaporator 8, simultaneously opening a reflux valve 24 of the first-stage hydrocyclone, automatically adjusting the liquid level of the first-stage hydrocyclone 9 according to liquid level interlocking, feeding the first-stage hydrocyclone to a flash tank 10 under the self-pressure, and automatically evaporating in the flash tank 10; when the density of the materials in the flash tank 10 reaches 1.35g/cm3, starting a flash pump 25 to feed the concentrated solution into a concentrated solution storage tank 11, when the liquid level reaches a certain height, opening a crystallizing tank feeding valve 29, starting a concentrated solution pump 26 to feed the materials into a crystallizing tank 12, when the liquid level of the crystallizing tank 12 reaches a certain height, starting the crystallizing tank to stir 30, and cooling and crystallizing the materials by using circulating water; when crystal particles are separated out from the crystallization tank 12, a crystallization tank discharge valve 31 is opened to feed materials into the centrifugal separator 13, the materials are conveyed to a packaging machine 15 through a belt 14 to be packaged after centrifugal separation, and mother liquor enters a mother liquor pit 16 and returns to the I-effect evaporator 7 through a pit pump 27 to be recycled.
The above is the preferred embodiment of the present invention, and the technical personnel in the field of the present invention can also change and modify the above embodiment, therefore, the present invention is not limited to the above specific embodiment, and any obvious improvement, replacement or modification made by the technical personnel in the field on the basis of the present invention all belong to the protection scope of the present invention.
Claims (4)
1. The utility model provides a device of wet-type magnesium oxide method desulfurization waste liquid concentration recovery magnesium sulfate heptahydrate which characterized in that: the device comprises an impurity removing agent liquid tank (1), a desulfurization liquid storage tank (2), an impurity removing reactor (3), a desulfurization liquid intermediate tank (4), a plate-and-frame filter press (5), a desulfurization clear liquid storage tank (6), a first-effect evaporator (7), a second-effect evaporator (8), a first-stage hydrocyclone separator (9), a flash tank (10), a concentrated liquid tank (11), a crystallizing tank (12), a centrifugal separator (13), a packing machine (15) and a mother liquid pit (16); the device is characterized in that an impurity removing agent liquid tank (1) and a desulfurizing liquid storage tank (2) are respectively connected with an impurity removing reactor (3) through a bottom liquid drainage pipeline, the impurity removing reactor (3) is connected with a desulfurizing liquid intermediate tank (4) through a bottom liquid drainage pipeline, the desulfurizing liquid intermediate tank (4) is connected with a plate-and-frame filter press (5) through a filter press pump (18) arranged at the bottom of the desulfurizing liquid intermediate tank, the plate-and-frame filter press (5) is connected with a desulfurizing clear liquid storage tank (6) through a bottom liquid drainage pipeline, the desulfurizing clear liquid storage tank (6) is connected with an I-effect evaporator (7) through a feed pump (19) arranged at the bottom of the desulfurizing clear liquid intermediate tank, the I-effect evaporator (7) is connected with a II-effect evaporator (8) through an I-effect material passing pump (21) arranged at the bottom of the I-effect evaporator (7), the I-effect evaporator (7) is connected with a steam main pipe through a steam valve (20), secondary steam generated by the I-effect evaporator (7) is connected with the II-effect evaporator (8) through a top steam pipeline, II effect evaporator (8) tops are passed through the bleed line and are linked to each other with vacuum pump (28), II effect evaporator (8) are crossed material pump (23) and are linked to each other with one-level hydrocyclone (9) through II effects that set up in its bottom, one-level hydrocyclone (9) link to each other with flash tank (10) through bottom drainage tube, flash tank (10) link to each other with concentrate jar (11) through flash pump (25) that set up in its bottom, concentrate jar (11) link to each other with crystallizer (12) through concentrate pump (26) that set up in its bottom, crystallizer (12) are equipped with crystallizer stirring (30) and crystallizer blow-off valve (31), and crystallizer (12) link to each other with centrifuge (13) through its bottom drainage tube, centrifuge (13) lower part is provided with belt (14), and belt (14) link to each other with packagine machine (15), and a mother liquor pipeline at the bottom of the centrifugal separator (13) is connected with a mother liquor pit (16), and the mother liquor pit (16) returns to the I-effect evaporator (7) through a pit pump (27).
2. The device for concentrating and recovering magnesium sulfate heptahydrate from the wet magnesium oxide desulfurization waste liquid according to claim 1, characterized in that: a doctor solution delivery pump (17) is arranged between the doctor solution storage tank (2) and the impurity removal reactor (3).
3. The device for concentrating and recovering magnesium sulfate heptahydrate from the wet magnesium oxide desulfurization waste liquid according to claim 1, characterized in that: the outlet of the feed pump (19) is provided with an automatic discharge valve (32) and a liquid level interlock of the first-effect evaporator (7), an automatic material stringing valve (22) is arranged on a material passing pipeline between the first-effect evaporator (7) and the second-effect evaporator (8), the automatic material stringing valve (22) is interlocked with the liquid level of the second-effect evaporator (8), and the top of the first-stage hydrocyclone separator (9) is provided with a reflux valve (24) which is connected with a feed pipeline of the second-effect evaporator (8).
4. The device for concentrating and recovering magnesium sulfate heptahydrate from the wet magnesium oxide desulfurization waste liquid according to claim 1, characterized in that: a densitometer (33) provided in the outlet line of the flash tank (10) is interlocked with a crystallizer feed valve (29) provided in the crystallizer (12).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022687948.2U CN214087744U (en) | 2020-11-19 | 2020-11-19 | Device for concentrating and recovering magnesium sulfate heptahydrate from wet magnesium oxide desulfurization waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022687948.2U CN214087744U (en) | 2020-11-19 | 2020-11-19 | Device for concentrating and recovering magnesium sulfate heptahydrate from wet magnesium oxide desulfurization waste liquid |
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| Publication Number | Publication Date |
|---|---|
| CN214087744U true CN214087744U (en) | 2021-08-31 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022687948.2U Active CN214087744U (en) | 2020-11-19 | 2020-11-19 | Device for concentrating and recovering magnesium sulfate heptahydrate from wet magnesium oxide desulfurization waste liquid |
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| Country | Link |
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| CN (1) | CN214087744U (en) |
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2020
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Effective date of registration: 20240220 Address after: 737100 No. 2 Lanzhou Road, Beijing Road Street, Jinchuan District, Jinchang City, Gansu Province Patentee after: Jinchuan Group Nickel Cobalt Co.,Ltd. Country or region after: China Address before: 737100 Beijing Road, Jinchang City, Gansu Province Patentee before: JINCHUAN GROUP Co.,Ltd. Country or region before: China |